Processes for production and purification of hydrofluoroolefins

ABSTRACT

Disclosed herein are processes for the production of hydrofluoroolefins including 2,3,3,4,4,4-hexafluoro-1-butene by dehydrofluorination. Also disclosed herein are processes for separation of hydrofluoroolefins from hydrofluorocarbons and from hydrogen fluoride.

CROSS-REFERENCE TO RELATED APPLICATIONS

This application is a continuation application claiming priority benefit of U.S. patent application Ser. No. 13/013,065, filed Jan. 25, 2011, which is a divisional application claiming priority benefit of U.S. patent application Ser. No. 11/264,183, filed Nov., 1, 2005, now U.S. Pat. No. 7,897,823, which is a continuation-in-part of and claims priority benefit of U.S. patent application Ser. No. 11/259,901 filed Oct. 27, 2005, now abandoned, which claims the benefit of U.S. Provisional Patent Application No. 60/623,210, filed Oct. 29, 2004, all of which are incorporated herein by reference in their entireties.

BACKGROUND OF THE INVENTION

1. Field of the Invention

The present disclosure relates to the field of production and purification of hydrofluoroolefin compounds. The present disclosure further relates to processes utilizing azeotrope compositions for separation of hydrofluoroolefins from hydrofluorocarbons and hydrogen fluoride.

2. Description of Related Art

Chlorine-containing compounds such as chlorofluorocarbons (CFCs) are considered to be detrimental to the Earth's ozone layer. Many of the hydrofluorocarbons (HFCs), used to replace CFCs, have been found to contribute to global warming. Therefore, there is a need to identify new compounds that do not damage the environment, but also possess the properties necessary to function as refrigerants, solvents, cleaning agents, foam blowing agents, aerosol propellants, heat transfer media, dielectrics, fire extinguishing agents, sterilants and power cycle working fluids. Fluorinated olefins, especially those containing one or more hydrogens in the molecule (referred to herein as hydrofluoroolefins) are being considered for use in some of these applications such as in refrigeration as well as in processes to make fluoropolymers.

1,1,3,3,3-Pentafluoropropene is a useful cure-site monomer in polymerizations to form fluoroelastomers. U.S. Pat. Nos. 6,703,533, 6,548,720, 6,476,281, 6,369,284, 6,093,859, and 6,031,141, as well as published Japanese patent applications JP 09095459 and JP 09067281, and WIPO publication WO 2004018093, disclose processes wherein 1,1,1,3,3,3-hexafluoropropane is heated at temperatures below 500° C. in the presence of catalyst to form 1,1,3,3,3-pentafluoropropene. These low-temperature catalytic routes are chosen because of the well-known tendency for fluorocarbons to fragment at higher temperatures, e.g., above 500° C. This is made clear in Chemistry of Organic Fluorine Compounds, by Milos Hudlicky, 2^(nd) Revised Edition, Ellis Horwood PTR Prentice Hall p. 515: “Polyfluoroparaffins and especially fluorocarbons and other perfluoro derivates show remarkable heat stability. They usually do not decompose at temperatures below 300° C. Intentional decomposition, however, carried out at temperatures of 500-800° C., causes all possible splits in their molecules and produces complex mixtures which are difficult to separate.”

U.S. Patent Application Publication 2002/0032356 discloses a process for producing the perfluorinated monomers tetrafluoroethylene and hexafluoropropylene in a gold-lined pyrolysis reactor.

The catalytic process has disadvantages, including catalyst preparation, start-up using fresh catalyst, catalyst deactivation, potential for plugging of catalyst-packed reactors with polymeric by-products, catalyst disposal or reactivation, and long reaction times that impose a space/time/yield reactor penalty. It would be desirable to be able to produce 1,1,3,3,3-pentafluoropropene from 1,1,1,3,3,3-hexafluoropropane in high yield by a non-catalytic process.

BRIEF SUMMARY OF THE INVENTION

One aspect relates to a process to produce a hydrofluoroolefin comprising dehydrofluorinating a hydrofluorocarbon containing at least one hydrogen and at least one fluorine on adjacent carbons, thereby forming a product mixture comprising said hydrofluoroolefin, unreacted hydrofluorocarbon and hydrogen fluoride, wherein at least one of said hydrofluoroolefin and said hydrofluorocarbon are present in said product mixture as an azeotrope composition with hydrogen fluoride.

A further aspect relates to a process for the separation of a hydrofluoroolefin from a hydrofluorocarbon wherein said hydrofluoroolefin contains one less fluorine atom and one less hydrogen atom than said hydrofluorocarbon, said process comprising: a) forming a mixture comprising hydrofluoroolefin, hydrofluorocarbon, and hydrogen fluoride; and b) subjecting said mixture to a distillation step forming a column distillate composition comprising an azeotrope or near-azeotrope composition of hydrogen fluoride and hydrofluoroolefin essentially free of said hydrofluorocarbon.

A further aspect relates to a process to produce a hydrofluoroolefin comprising: a) feeding a hydrofluorocarbon containing at least one hydrogen and at least one fluorine on adjacent carbons to a reaction zone for dehydrofluorination to form a reaction product composition comprising hydrofluoroolefin, unreacted hydrofluorocarbon and hydrogen fluoride; b) subjecting said reaction product composition to a first distillation step to form a first distillate composition comprising an azeotrope or near-azeotrope composition containing hydrofluoroolefin and hydrogen fluoride and a first bottoms composition comprising hydrofluorocarbon; c) subjecting said first distillate composition to a second distillation step from which a composition enriched in either (i) hydrogen fluoride or (ii) hydrofluoroolefin is removed as a second distillate composition with a second bottoms composition being enriched in the other of said components (i) or (ii); and d) subjecting said second distillate composition to a third distillation step conducted at a different pressure than the second distillation step in which the component enriched in the second bottoms composition in (c) is removed as a third distillate composition with the third bottoms composition of the third distillation step enriched in the same component that was enriched in the second distillate composition.

BRIEF DESCRIPTION OF THE DRAWING(S)

FIG. 1 is a schematic flow diagram illustrating one embodiment for practicing a two-column azeotropic distillation process.

FIG. 2 is a schematic flow diagram illustrating one embodiment for practicing a process for production of hydrofluoroolefin.

DETAILED DESCRIPTION OF THE INVENTION

One aspect relates to processes to produce and processes to purify hydrofluoroolefins. The processes to purify include processes to separate hydrofluoroolefins from hydrogen fluoride and processes to separate hydrofluoroolefins from hydrofluorocarbons and hydrogen fluoride, said processes utilizing azeotrope or near-azeotrope compositions.

A further aspect provides a process to produce a hydrofluoroolefin comprising dehydrofluorinating a hydrofluorocarbon containing at least one hydrogen and at least one fluorine on adjacent carbons, thereby forming a product mixture comprising said hydrofluoroolefin, unreacted hydrofluorocarbon and hydrogen fluoride, wherein at least one of said hydrofluoroolefin and said hydrofluorocarbon are present in said product mixture as an azeotrope composition with hydrogen fluoride.

The hydrofluoroolefins are acyclic compounds containing 3 to 8 carbon atoms, fluorine and hydrogen. Hydrofluoroolefins must also contain at least one double bond and may be linear or branched. The acyclic hydrofluoroolefins may be represented by the formula, C_(x)H_(a-1)F_(b-2), wherein x is an integer from 3 to 8, a is an integer from 2 to (x+1), b is an integer from (x+1) to (2×) and wherein a+b=2x+2. Representative hydrofluoroolefins include, but are not limited to, trifluoropropenes, tetrafluoropropenes, pentafluoropropenes, tetrafluorobutenes, pentafluorobutenes, hexafluorobutenes, heptafluorobutenes, pentafluoropentenes, hexafluoropentenes, heptafluoropentenes, octafluoropentenes, nonafluoropentenes, hexafluorohexenes, heptafluorohexenes, octafluorohexenes, nonafluorohexenes, decafluorohexenes, undecafluorohexenes, heptafluoroheptenes, octafluoroheptenes, nonafluoroheptenes, decafluoroheptenes, undecafluoroheptenes, dodecafluoroheptenes, tridecafluoroheptenes, octafluorooctenes, nonafluorooctenes, decafluorooctenes, undecafluorooctenes, dodecafluorooctenes, tridecafluorooctenes, tetradecafluorooctenes, and pentadecafluorooctenes.

Also included are cyclic hydrofluoroolefins containing a total of 4 to 8 carbon atoms including 4 to 6 carbon atoms in the ring. Cyclic hydrofluoroolefins must also contain at least one double bond and may have branching on the ring. The cyclic hydrofluoroolefins may be represented by the formula, C_(y)H_(c-1)F_(d-1), wherein y is an integer from 4 to 8, c is an integer from 2 to y, d in an integer from y to (2y-2) and wherein c+d=2y. Representative cyclic hydrofluoroolefins include, but are not limited to, difluorocyclopropenes, trifluorocyclopropenes, trifluorocyclobutenes, tetrafluorocyclobutenes, pentafluorocyclobutenes, trifluoromethylcyclopropenes, tetrafluoromethylcyclopropenes, pentafluoromethylcyclopropenes, tetrafluorocyclopentenes, pentafluorocyclopentenes, hexafluorocyclopentenes, heptafluorocyclopentenes, tetrafluorodimethylcyclopropenes, pentafluorodimethylcyclopropenes, hexafluorodimethylcyclopropenes, heptafluorodimethylcyclopropenes, tetrafluoroethylcyclopropenes, pentafluoroethylcyclopropenes, hexafluoroethylcyclopropenes, heptafluoroethylcyclopropenes, tetrafluoromethylcyclobutenes, pentafluoromethylcyclobutenes, hexafluoromethylcyclobutenes, heptafluoromethylcyclobutenes, pentafluorocyclohexenes, hexafluorocyclohexenes, heptafluorocyclohexenes, octafluorocyclohexenes, nonafluorocyclohexenes, pentafluoromethylcyclopentenes, hexafluoromethylcyclopentenes, heptafluoromethylcyclopentenes, octafluoromethylcyclopentenes, nonafluoromethylcyclopentenes, pentafluorodimethylcyclobutenes, hexafluorodimethylcyclobutenes, heptafluorodimethylcyclobutenes, octafluorodimethylcyclobutenes, nonafluorodimethylcyclobutenes, pentafluoroethylcyclobutenes, hexafluoroethylcyclobutenes, heptafluoroethylcyclobutenes, octafluoroethylcyclobutenes, nonafluoroethylcyclobutenes, pentafluorotrimethylcyclopropenes, hexafluorotrimethylcyclopropenes, heptafluorotrimethylcyclopropenes, octafluorotrimethylcyclopropenes, and nonafluorotrimethylcyclopropenes.

The hydrofluoroolefins may exist as different configurational isomers or stereoisomers. Included are all single configurational isomers, single stereoisomers or any combination thereof. For instance, HFC-1234ze (CF₃CH═CHF) is meant to represent the E-isomer, Z-isomer, or any combination or mixture of both isomers in any ratio. Another example is HFC-1336m/z (CF₃CH═CHCF₃), by which is represented the E-isomer, Z-isomer, or any combination or mixture of both isomers in any ratio.

The hydrofluorocarbons are acyclic, linear or branched compounds containing 3 to 8 carbon atoms, hydrogen and fluorine. At least one hydrogen atom and at least one fluorine atom must be on adjacent carbon atoms. The hydrofluorocarbons may be represented by the formula C_(x)H_(a)F_(b), wherein x is an integer from 3 to 8, a is an integer from 2 to (x+1), b is an integer from (x+1) to (2×) and wherein a+b=2x+2. The hydrofluorocarbons are precursor compounds for the hydrofluoroolefins. The hydrofluorocarbons may be dehydrofluorinated in the vapor phase to form the hydrofluoroolefins of the present invention along with hydrogen fluoride co-product.

Also included are cyclic hydrofluorocarbons containing a total of 4 to 8 carbon atoms and with the ring comprising 4 to 6 carbon atoms. At least one hydrogen atom and at least one fluorine atom must be on adjacent carbon atoms. The cyclic hydrofluorocarbons may be represented by the formula C_(y)H_(c)F_(d), wherein y is an integer from 4 to 8, c is an integer from 2 to y, d is an integer from y to (2y-2) and wherein c+d=2y. The cyclic hydrofluorocarbons are precursor compounds for the cyclic hydrofluoroolefins. The cyclic hydrofluorocarbons may be dehydrofluorinated in the vapor phase to form the cyclic hydrofluoroolefins of the present invention along with hydrogen fluoride co-product.

The list in Table 1 indicates representative hydrofluoroolefins and the corresponding precursor hydrofluorocarbons. The list in Table 2 indicates representative cyclic hydrofluoroolefins and the corresponding precursor cyclic hydrofluorocarbons. Depending on the number and position of hydrogen and fluorine atoms in a particular precursor hydrofluorocarbon, and provided that at least one hydrogen atom and at least one fluorine atom must be on adjacent carbon atoms, more than one hydrofluoroolefin may be produced. Tables 1 and 2 indicate one representative hydrofluoroolefin from a precursor hydrofluorocarbon and in some instances more than one hydrofluoroolefin from a precursor hydrofluorocarbon.

TABLE 1 Hydrofluorocarbon Hydrofluoroolefin(s) CF₃CF₂CH₂F CF₃CF═CHF CF₃CHFCHF₂ CF₃CF═CHF CF₃CH₂CF₃ CF₃CH═CF₂ CHF₂CF₂CH₂F CHF₂CF═CHF CHF₂CHFCHF₂ CHF₂CF═CHF CF₃CF₂CH₃ CF₃CF═CH₂ CF₃CHFCH₂F CF₃CF═CH₂ CF₃CH₂CHF₂ CF₃CH═CHF CH₂FCF₂CH₂F CH₂FCF═CHF CH₃CF₂CHF₂ CHF₂CF═CH₂ CHF₂CHFCH₂F CHF₂CF═CH₂ CF₃CH₂CH₂F CF₃CH═CH₂ CF₃CHFCH₃ CF₃CH═CH₂ CHF₂CH₂CHF₂ CHF₂CH═CHF CH₂FCF₂CF₂CF₃ CHF═CFCF₂CF₃ CF₃CHFCF₂CHF₂ CF₃CF═CFCHF₂ CF₃CH₂CF₂CF₃ CF₃CH═CFCF₃ CF₃CHFCHFCF₃ CF₃CH═CFCF₃ CH₃CF₂CF₂CF₃ CH₂═CFCF₂CF₃ CH₂FCHFCF₂CF₃ CH₂═CFCF₂CF₃ CF₃CHFCF₂CH₂F CF₃CF═CFCH₂F CH₂FCF₂CF₂CHF₂ CHF═CFCF₂CHF₂ CHF₂CH₂CF₂CF₃ CHF₂CH═CFCF₃ CHF₂CHFCHFCF₃ CHF₂CF═CHCF₃ and/or CHF₂CH═CFCF₃ CHF₂CHFCF₂CHF₂ CHF₂CF═CFCHF₂ CHF₂CF₂CH₂CF₃ CHF₂CF═CHCF₃ CF₃CH₂CHFCF₃ CF₃CH═CHCF₃ CF₃CHFCF₂CH₃ CF₃CF═CFCH₃ CF₃CF₂CHFCH₃ CF₃CF═CFCH₃ CH₃CF₂CF₂CHF₂ CH₂═CFCF₂CHF₂ CF₃CH₂CF₂CH₂F CF₃CH═CFCH₂F CF₃CF₂CH₂CH₂F CF₃CF═CHCH₂F and/or CF₃CF₂CH═CH₂ CH₂FCHFCHFCF₃ CH₂FCF═CHCF₃ and/or CH₂FCH═CFCF₃ CHF₂CF₂CHFCH₂F CHF₂CF═CFCH₂F and/or CHF₂CF₂CF═CH₂ CF₃CH₂CH₂CF₃ CF₃CH₂CH═CF₂ CHF₂CH₂CHFCF₃ CHF₂CH═CHCF₃ CHF₂CHFCH₂CF₃ CHF₂CH═CHCF₃ CHF₂CH₂CF₂CHF₂ CHF₂CH═CFCHF₂ CHF₂CHFCHFCHF₂ CHF₂CH═CFCHF₂ CF₃CF₂CH₂CH₃ CF₃CF═CHCH₃ CF₃CH₂CF₂CH₃ CF₃CH═CFCH₃ CH₃CHFCHFCF₃ CH₃CF═CHCF₃ and/or CH₃CH═CFCF₃ CH₃CHFCF₂CHF₂ CH₃CF═CFCHF₂ CH₂FCH₂CHFCF₃ CH₂FCH═CHCF₃ CH₂FCHFCH₂CF₃ CH₂FCH═CHCF₃ CH₂FCH₂CF₂CHF₂ CH₂FCH═CFCHF₂ CH₂FCHFCHFCHF₂ CH₂FCF═CHCHF₂ and/or CH₂FCH═CFCHF₂ CHF₂CH₂CH₂CF₃ CHF═CHCH₂CF₃ CHF₂CH(CF₃)₂ CHF═C(CF₃)₂ CH₂FCF(CF₃)₂ CHF═C(CF₃)₂ CH₃CF(CF₃)₂ CH₂═C(CF₃)₂ CH₂FCH(CF₃)₂ CH₂═C(CF₃)₂ CHF₂CF(CHF₂)₂ CF₂═C(CHF₂)₂ CH₃CH(CF₃)₂ CF₂═C(CF₃)CH₃ CF₃CH(CH₂F)₂ CH₂═C(CF₃)CH₂F CHF₂CH(CHF₂)₂ CHF═C(CHF₂)₂ CH₃CF(CHF₂)₂ CH₂═C(CHF₂)₂ CH₂FCH(CH₂F)CF₃ CH₂═C(CH₂F)CF₃ CH₂FCH(CHF₂)₂ CH₂═C(CHF₂)₂ CF₃CHFCHFCF₂CF₃ CF₃CH═CFCF₂CF₃ and/or CF₃CF═CHCF₂CF₃ CF₃CF₂CH₂CF₂CF₃ CF₃CF₂CH═CFCF₃ CF₃CH₂CF₂CF₂CF₃ CF₃CH═CFCF₂CF₃ CF₃CH₂CHFCF₂CF₃ CF₃CH═CHCF₂CF₃ CF₃CHFCH₂CF₂CF₃ CF₃CH═CHCF₂CF₃ CH₃CF₂CF₂CF₂CF₃ CH₂═CFCF₂CF₂CF₃ CH₃CF₂CF₂CF₂CHF₂ CH₂═CFCF₂CF₂CHF₂ CF₃CH₂CF₂CH₂CF₃ CF₃CH═CFCH₂CF₃ CHF₂CF₂CF₂CHFCH₃ CHF₂CF₂CF═CFCH₃ CF₃CF₂CF₂CH₂CH₃ CF₃CF₂CF═CHCH₃ (CF₃)₂CFCH₂CF₃ (CF₃)₂C═CHCF₃ (CF₃)₂CHCHFCF₃ (CF₃)₂C═CHCF₃ (CF₃)₂CFCHFCHF₂ (CF₃)₂C═CFCHF₂ (CF₃)₂CFCH₂CHF₂ (CF₃)₂C═CHCHF₂ (CF₃)₂CFCH₂CH₃ (CF₃)₂C═CHCH₃ CF₃CF₂CHFCHFCF₂CF₃ CF₃CF₂CH═CFCF₂CF₃ CH₂FCHFCF₂CF₂CF₂CF₃ CH₂═CFCF₂CF₂CF₂CF₃ CF₃CH₂CHFCF₂CF₂CF₃ CF₃CH═CHCF₂CF₂CF₃ CF₃CHFCH₂CF₂CF₂CF₃ CF₃CH═CHCF₂CF₂CF₃ CF₃CF₂CH₂CHFCF₂CF₃ CF₃CF₂CH═CHCF₂CF₃ CF₃CH₂CF₂CF₂CH₂CF₃ CF₃CH═CFCF₂CH₂CF₃ CF₃CF₂CH₂CH₂CF₂CF₃ CF₃CF═CHCH₂CF₂CF₃ CH₃CH₂CF₂CF₂CF₂CF₃ CH₃CH═CFCF₂CF₂CF₃ CH₃CHFCF₂CF₂CF₂CF₃ CH₂═CHCF₂CF₂CF₂CF₃ CF₃CF₂CF₂CH₂CHFCH₃ CF₃CF₂CF₂CH═CHCH₃ (CF₃)₂CFCF₂CH₂CH₃ (CF₃)₂CFCF═CHCH₃ (CF₃)₂CFCH₂CH₂CH₃ (CF₃)₂C═CHCH₂CH₃ (CF₃)₂CHCHFCF₂CF₃ (CF₃)₂C═CHCF₂CF₃ (CF₃)₂CFCHFCHFCF₃ (CF₃)₂C═CFCHFCF₃ and/or (CF₃)₂CFCF═CHCF₃ and/or (CF₃)₂CFCH═CFCF₃ (CF₃)₂CHCH₂CF₂CF₃ (CF₃)₂CHCH═CFCF₃ (CF₃)₂CFCH(CH₃)₂ (CF₃)₂C═C(CH₃)₂ (CH₃)₂CHCF₂CF₂CF₃ (CH₃)₂C═CFCF₂CF₃ C₂F₅CHFCHFCF₂C₂F₅ C₂F₅CF═CHCF₂C₂F₅ and/or C₂F₅CH═CFCF₂C₂F₅ CF₃CHFCHFCF₂CF₂C₂F₅ CF₃CF═CHCF₂CF₂C₂F₅ and/or CF₃CH═CFCF₂CF₂C₂F₅ C₂F₅CHFCH₂CF₂C₂F₅ C₂F₅CH═CHCF₂C₂F C₂F₅CH₂CHFCF₂C₂F₅ C₂F₅CH═CHCF₂C₂F₅ CF₃CHFCH₂CF₂CF₂C₂F₅ CF₃CH═CHCF₂CF₂C₂F₅ CF₃CH₂CHFCF₂CF₂C₂F₅ CF₃CH═CHCF₂CF₂C₂F₅ CHF₂CF₂CF₂CF₂CF₂CF₂CH₃ CHF₂CF₂CF₂CF₂CF₂CF═CH₂ CF₃CF₂CF₂CF₂CF₂CH₂CH₃ CF₃CF₂CF₂CF₂CF═CHCH₃ CF₃CF₂CF₂CF₂CH₂CH₂CH₃ CF₃CF₂CF₂CF═CHCH₂CH₃ CF₃CF₂C(CH₃)HCH₂CF₂CF₃ CF₃CF₂CH(CH₃)CH═CFCF₃ (CH₃)₂CHCF₂CF₂CF₂CF₃ (CH₃)₂C═CFCF₂CF₂CF₃ C₂F₅CHFCHFCF₂CF₂C₂F₅ C₂F₅CF═CHCF₂CF₂C₂F₅ and/or C₂F₅CH═CFCF₂CF₂C₂F₅ C₂F₅CF₂CHFCHFCF₂C₂F₅ C₂F₅CF₂CF═CHCF₂C₂F₅ CF₃(CF₂)₅CH₂CH₂F CF₃(CF₂)₅CH═CH₂ CF₃(CF₂)₅CH₂CH₃ CF₃(CF₂)₄CF═CHCH₃ CF₃(CF₂)₃CH₂CH₂CHFCH₃ CF₃(CF₂)₃CH₂CH₂CH═CH₂ and/or CF₃(CF₂)₃CH₂CH═CHCH₃

TABLE 2 Hydrofluorocarbon Hydrofluoroolefin cyclo-CF₂CF₂CF₂CH₂— cyclo-CF₂CF₂CF═CH— cyclo-CF₂CF₂CHFCHF— cyclo-CF₂CF₂CF═CH— cyclo-CF₂CF₂CH₂CH₂— cyclo-CF₂CH₂CH═CF— cyclo-CF₂CF₂CF₂CHFCHF— cyclo-CF₂CF₂CF₂CF═CH— cyclo- cyclo-CF₂CF₂CF₂CF₂CF═CH— CF₂CF₂CF₂CF₂CHFCHF— cyclo- cyclo-CF₂CF₂CHFCF₂CF═CF— CF₂CF₂CHFCF₂CF₂CHF—

The hydrofluorocarbons are available commercially, may be made by methods known in the art, or may be made as described herein.

1,1,1,2,3,3-Hexafluoro-2-(trifluoromethyl)-pentane ((CF₃)₂CFCF₂CH₂CH₃) may be prepared by the reaction of 1,1,1,2,3,3-hexafluoro-2-(trifluoromethyl)-3-iodo-propane with ethylene to give 1,1,1,2,3,3-hexafluoro-2-(trifluoromethyl)-5-iodopentane followed by zinc reduction in an acid such as HCl or acetic acid.

1,1,1,2-Tetrafluoro-2-(trifluoromethyl)-pentane ((CF₃)₂CFCH₂CH₂CH₃) may be prepared by reacting methyl perfluoroisobutyrate with ethyl magnesium bromide followed by hydrolysis to give 1,1,1,2-tetrafluoro-2-(trifluoromethyl)-3-pentanol. The pentanol is converted to 4,5,5,5-tetrafluoro-4-(trifluoromethyl)-2-pentene by dehydration with phosphorous pentoxide and the double bond saturated by hydrogenation over a palladium on carbon catalyst.

1,1,1,2,2,3,3,4,4,5,5-Undecafluoroheptane (CF₃CF₂CF₂CF₂CF₂CH₂CH₃) may be prepared by reaction of 1,1,1,2,2,3,3,4,4,5,5-undecafluoro-5-iodo-pentane with ethylene to give 1,1,1,2,2,3,3,4,4,5,5-undecafluoro-7-iodo-heptane followed by zinc reduction in an acid such as HCl or acetic acid.

As mentioned earlier, certain precursor hydrofluorocarbons listed in Tables 1 and also in Table 2 may produce a single hydrofluoroolefin or a mixture of 2 or more hydrofluoroolefins as a result of the dehydrofluorination reaction. Included are the pairs of the hydrofluorocarbon and each hydrofluoroolefin individually or the hydrofluorocarbon and the mixtures of 2 or more hydrofluoroolefin compounds that may be produced by any specific reaction.

Anhydrous hydrogen fluoride (HF) is also useful in the processes and is commercially available.

One aspect relates to a process to produce a hydrofluoroolefin comprising dehydrofluorinating a hydrofluorocarbon containing at least one hydrogen and at least one fluorine on adjacent carbons, thereby forming a product mixture comprising said hydrofluoroolefin, unreacted hydrofluorocarbon and hydrogen fluoride, wherein at least one of said hydrofluoroolefin and said hydrofluorocarbon are present in said product mixture as an azeotrope composition with hydrogen fluoride.

The dehydrofluorination of a hydrofluorocarbon may be carried out in the vapor phase. Vapor phase dehydrofluorination of a hydrofluorocarbon may be suitably carried out using typical dehydrofluorination catalysts. Generally, the present dehydrofluorination may be carried out using any dehydrofluorination catalyst known in the art. These catalysts include, but are not limited to, aluminum fluoride; fluorided alumina; metals on aluminum fluoride; metals on fluorided alumina; oxides, fluorides, and oxyfluorides of magnesium, zinc and mixtures of magnesium and zinc and/or aluminum; lanthanum oxide and fluorided lanthanum oxide; chromium oxides, fluorided chromium oxides, and cubic chromium trifluoride; carbon, acid-washed carbon, activated carbon, three dimensional matrix carbonaceous materials; and metal compounds supported on carbon. The metal compounds are oxides, fluorides, and oxyfluorides of at least one metal selected from the group consisting of sodium, potassium, rubidium, cesium, yttrium, lanthanum, cerium, praseodymium, neodymium, samarium, chromium, iron, cobalt, rhodium, nickel, copper, zinc, and mixtures thereof.

Dehydrofluorination catalysts include aluminum fluoride, fluorided alumina, metals on aluminum fluoride, and metals on fluorided alumina, as disclosed in U.S. Pat. No. 5,396,000, incorporated herein by reference. Fluorided alumina and aluminum fluoride can be prepared as described in U.S. Pat. No. 4,902,838, incorporated herein by reference. Suitable metals include chromium, magnesium (e.g., magnesium fluoride), Group VIIB metals (e.g., manganese), Group IIIB metals (e.g., lanthanum), and zinc. In use, such metals are normally present as halides (e.g., fluorides), as oxides and/or as oxyhalides. Metals on aluminum fluoride and metals on fluorided alumina can be prepared by procedures as described in U.S. Pat. No. 4,766,260, incorporated herein by reference. In one embodiment, when supported metals are used, the total metal content of the catalyst is from about 0.1 to 20 percent by weight, typically from about 0.1 to 10 percent by weight. Preferred catalysts include catalysts consisting essentially of aluminum fluoride and/or fluorided alumina.

Additionally, dehydrofluorination catalysts include oxides, fluorides, and oxyfluorides of magnesium, zinc and mixtures of magnesium and zinc and/or aluminum. A suitable catalyst may be prepared, for example by drying magnesium oxide until essentially all water is removed, e.g., for about 18 hours at about 100° C. The dried material is then transferred to the reactor to be used. The temperature is then gradually increased to about 400° C. while maintaining a flow of nitrogen through the reactor to remove any remaining traces of moisture from the magnesium oxide and the reactor. The temperature is then lowered to about 200° C. and a fluoriding agent, such as HF, or other vaporizable fluorine containing compounds such as HF, SF₄, CCl₃F, CCl₂F₃, CHF₃, CHClF₂ or CCl₂FCClF₂, optionally diluted with an inert gas such as nitrogen, is passed through the reactor. The inert gas or nitrogen can be gradually reduced until only HF or other vaporizable fluorine containing compounds is being passed through the reactor. At this point, the temperature can be increased to about 450° C. and held at that temperature to convert the magnesium oxide to a fluoride content corresponding to at least 40 percent by weight, e.g., for 15 to 300 minutes, depending on the fluoriding agent flowrate and the catalyst volume. The fluorides are in the form of magnesium fluoride or magnesium oxyfluoride; the remainder of the catalyst is magnesium oxide. It is understood in the art that fluoriding conditions such as time and temperature can be adjusted to provide higher than 40 percent by weight fluoride-containing material.

Another suitable procedure for the catalyst preparation is to add ammonium hydroxide to a solution of magnesium nitrate and, if present, zinc nitrate and/or aluminum nitrate. The ammonium hydroxide is added to the nitrate solution to a pH of about 9.0 to 9.5. At the end of the addition, the solution is filtered, the solid obtained is washed with water, dried and slowly heated to 500° C., where it is calcined. The calcined product is then treated with a suitable fluorine-containing compound as described above.

Yet another procedure for the preparation of metal (i.e., magnesium, optionally containing also zinc and/or aluminum) fluoride catalysts containing one or more metal fluorides is to treat an aqueous solution of the metal(s) halide(s) or nitrate(s) in deionized water with 48 percent aqueous HF with stirring. Stirring is continued overnight and the slurry evaporated to dryness on a steam bath. The dried solid is then calcined in air at 400° C. for about four hours, cooled to room temperature, crushed and sieved to provide material for use in catalyst evaluations.

Additionally, dehydrofluorination catalysts include lanthanum oxide and fluorided lanthanum oxide.

Suitable fluorided lanthanum oxide compositions may be prepared in any manner analogous to those known to the art for the preparation of fluorided alumina. For example, the catalyst composition can be prepared by fluorination of lanthanum oxide.

Suitable catalyst compositions may also be prepared by precipitation of lanthanum as the hydroxide, which is thereafter dried and calcined to form an oxide, a technique well known to the art. The resulting oxide can then be pretreated as described herein.

The catalyst composition can be fluorinated to the desired fluorine content by pretreatment with a fluorine-containing compound at elevated temperatures, e.g., at about 200° C. to about 450° C. The pretreatment with a vaporizable fluorine-containing compound such as HF, SF₄, CCl₃F, CCl₂F₃, CHF₃, CHClF₂ or CCl₂FCClF₂ can be done in any convenient manner including in the reactor which is to be used for carrying out the dehydrofluorination reaction. By vaporizable fluorine-containing compound is meant a fluorine containing compound which, when passed over the catalyst at the indicated conditions, will fluorinate the catalyst to the desired degree.

A suitable catalyst may be prepared, for example, by drying La₂O₃ until essentially all moisture is removed, e.g., for about 18 hours at about 400° C. The dried catalyst is then transferred to the reactor to be used. The temperature is then gradually increased to about 400° C. while maintaining a flow of N₂ through the reactor to remove any remaining traces of moisture from the catalyst and the reactor. The temperature is then lowered to about 200° C. and the vaporizable fluorine-containing compound is passed through the reactor. If necessary, nitrogen or other inert gases can be used as diluents. The N₂ or other inert diluents can be gradually reduced until only the vaporizable fluorine-containing compound is being passed through the reactor. At this point the temperature can be increased to about 450° C. and held at that temperature to convert the La₂O₃ to a fluorine content corresponding to at least 80 percent LaF₃ by weight, e.g., for 15 to 300 minutes, depending on the flow of the fluorine containing compound and the catalyst volume.

Another suitable procedure for the catalyst preparation is to add ammonium hydroxide to a solution of La(NO₃)₃6H₂O. The ammonium hydroxide is added to the nitrate solution to a pH of about 9.0 to 9.5. At the end of the addition, the solution is filtered, the solid obtained is washed with water, and slowly heated to about 400° C., where it is calcined. The calcined product is then treated with a suitable vaporizable fluorine-containing compound as described above.

Additionally, dehydrofluorination catalysts include chromium oxides, fluorided chromium oxides, and cubic chromium trifluoride. Cubic chromium trifluoride may be prepared from CrF₃XH₂O, where X is 3 to 9, preferably 4, by heating in air or an inert atmosphere (e.g., nitrogen or argon) at a temperature of about 350° C. to about 400° C. for 3 to 12 hours, preferably 3 to 6 hours.

Cubic chromium trifluoride is useful by itself, or together with other chromium compounds, as a dehydrofluorination catalyst. Preparation of cubic chromium trifluoride is described in U.S. Pat. No. 6,031,141, incorporated herein by reference. Of note are catalyst compositions comprising chromium wherein at least 10 weight percent of the chromium is in the form of cubic chromium trifluoride, particularly catalyst compositions wherein at least 25 percent of the chromium is in the form of cubic chromium trifluoride, and especially catalyst compositions wherein at least 60 percent of the chromium is in the form of cubic chromium trifluoride. The chromium, including the cubic chromium trifluoride can be supported on and/or physically mixed with materials such as carbon, aluminum fluoride, fluorided alumina, lanthanum fluoride, magnesium fluoride, calcium fluoride, zinc fluoride and the like. Preferred are combinations including cubic chromium trifluoride in combination with magnesium fluoride and/or zinc fluoride.

Additionally, dehydrofluorination catalysts include activated carbon, or three dimensional matrix carbonaceous materials as disclosed in U.S. Pat. No. 6,369,284, incorporated herein by reference; or carbon or metals such as sodium, potassium, rubidium, cesium, yttrium, lanthanum, cerium, praseodymium, neodymium, samarium, chromium, iron, cobalt, rhodium, nickel, copper, zinc, and mixtures thereof, supported on carbon as disclosed in U.S. Pat. No. 5,268,122, incorporated herein by reference. Carbon from any of the following sources are useful for the process of this invention; wood, peat, coal, coconut shells, bones, lignite, petroleum-based residues and sugar. Commercially available carbons which may be used include those sold under the following trademarks: Barneby & Sutcliffe™, Darco™, Nucharm, Columbia JXN™, Columbia LCK™, Calgon PCB, Calgon BPL™, Westvaco™, Norit™, and Barnaby Cheny NB™.

Carbon includes acid-washed carbon (e.g., carbon which has been treated with hydrochloric acid or hydrochloric acid followed by hydrofluoric acid). Acid treatment is typically sufficient to provide carbon that contains less than 1000 ppm of ash. Suitable acid treatment of carbon is described in U.S. Pat. No. 5,136,113, incorporated herein by reference. The carbon also includes three dimensional matrix porous carbonaceous materials. Examples are those described in U.S. Pat. No. 4,978,649, incorporated herein by reference. Of note are three dimensional matrix carbonaceous materials which are obtained by introducing gaseous or vaporous carbon-containing compounds (e.g., hydrocarbons) into a mass of granules of a carbonaceous material (e.g., carbon black); decomposing the carbon-containing compounds to deposit carbon on the surface of the granules; and treating the resulting material with an activator gas comprising steam to provide a porous carbonaceous material. A carbon-carbon composite material is thus formed.

The physical shape of the catalyst is not critical and may, for example, include pellets, powders or granules. Additionally, for catalysts supported on carbon, the carbon may be in the form of powder, granules, or pellets, or the like. Although not essential, catalysts that have not been fluorided may be treated with HF before use. It is thought that this converts some of the surface oxides to oxyfluorides. This pretreatment can be accomplished by placing the catalyst in a suitable container (which can be the reactor to be used to perform the reaction of the instant invention) and thereafter, passing HF over the dried catalyst so as to partially saturate the catalyst with HF. This is conveniently carried out by passing HF over the catalyst for a period of time (e.g., about 15 to 300 minutes) at a temperature of, for example, about 200° C. to about 450° C.

The catalytic dehydrofluorination may be suitably conducted at a temperature in the range of from about 200° C. to about 500° C., and, in another embodiment, from about 300° C. to about 450° C. The contact time is typically from about 1 to about 450 seconds, and, in another embodiment, from about 10 to about 120 seconds.

The reaction pressure can be subatmospheric, atmospheric or superatmostpheric. Generally, near atmospheric pressures are preferred. However, the dehydrofluorination can be beneficially run under reduced pressure (i.e., pressures less than one atmosphere).

The catalytic dehydrofluorination can optionally be carried out in the presence of an inert gas such as nitrogen, helium, or argon. The addition of an inert gas can be used to increase the extent of dehydrofluorination. Of note are processes where the mole ratio of inert gas to hydrofluorocarbon undergoing dehydrofluorination is from about 5:1 to about 1:1. Nitrogen is the preferred inert gas.

A further aspect provides a process for the manufacture of a hydrofluoroolefin by dehydrofluorination of a hydrofluorocarbon in a reaction zone at elevated temperature in the absence of catalyst.

In the present embodiment of dehydrofluorination, the dehydrofluorination of hydrofluorocarbon can be carried out in a reaction zone at an elevated temperature in the absence of a catalyst as described below in the description for the pyrolysis of CF₃CH₂CF₃ to CF₂═CHCF₃ and HF. Appropriate temperatures may be between about 350° C. and about 900° C., and, in another embodiment, between about 450° C. and about 900° C. The residence time of gases in the reaction zone is typically from about 0.5 to about 60 seconds, and, in another embodiment, from about 2 seconds to about 20 seconds.

The reaction pressure for the dehydrofluorination reaction at elevated temperature in the absence of catalyst may be subatmospheric, atmospheric, or superatmospheric. Generally, near atmospheric pressures are preferred. However, the dehydrofluorination can be beneficially run under reduced pressure (i.e., pressures less than one atmosphere).

The dehydrofluorination at an elevated temperature in the absence of a catalyst may optionally be carried out in the presence of an inert gas such as nitrogen, helium or argon. The addition of an inert gas can be used to increase the extent of dehydrofluorination. Of note are processes where the mole ratio of inert gas to the hydrofluorocarbon undergoing dehydrofluorination is from about 5:1 to about 1:1. Nitrogen is the preferred inert gas.

The reaction zone for either catalyzed or non-catalyzed dehydrofluorination may be a reaction vessel fabricated from nickel, iron, titanium or their alloys, as described in U.S. Pat. No. 6,540,933, incorporated herein by reference. A reaction vessel of these materials (e.g., a metal tube) optionally packed with the metal in suitable form may also be used. When reference is made to alloys, it is meant a nickel alloy containing from about 1 to about 99.9 weight percent nickel, an iron alloy containing about 0.2 to about 99.8 weight percent iron, and a titanium alloy containing about 72 to about 99.8 weight percent titanium. Of note is the use of an empty (unpacked) reaction vessel made of nickel or alloys of nickel such as those containing about 40 weight percent to about 80 weight percent nickel, e.g., Inconel™ 600 nickel alloy, Hastelloy™ C617 nickel alloy or Hastelloy™ C276 nickel alloy.

When used for packing, the metal or metal alloys may be particles or formed shapes such as, for example, perforated plates, rings, wire, screen, chips, pipe, shot, gauze, or wool.

The product mixture resulting from the dehydrofluorination of hydrofluorocarbon will contain hydrofluoroolefin, unreacted hydrofluorocarbon and hydrogen fluoride. The amount of unreacted hydrofluorocarbon will depend upon the percent conversion achieved in the reaction.

It has been discovered and is disclosed in co-owned, co-pending U.S. provisional patent applications, attorney docket numbers FL-1158, FL-1160, FL-1161, FL-1169, FL-1188 and FL-1195, that hydrofluoroolefins may form azeotrope or near-azeotrope compositions with hydrogen fluoride. These azeotrope and near-azeotrope compositions are useful in processes to produce hydrofluoroolefins and in processes to separate hydrofluoroolefins from hydrogen fluoride and hydrofluorocarbons.

As recognized in the art, an azeotrope or a near-azeotrope composition is an admixture of two or more different components which, when in liquid form under a given pressure, will boil at a substantially constant temperature, which temperature may be higher or lower than the boiling temperatures of the individual components, and which will provide a vapor composition essentially identical to the liquid composition undergoing boiling.

For the purpose of this discussion, near-azeotrope composition (also commonly referred to as an “azeotrope-like composition”) means a composition that behaves like an azeotrope (i.e., has constant boiling characteristics or a tendency not to fractionate upon boiling or evaporation). Thus, the composition of the vapor formed during boiling or evaporation is the same as or substantially the same as the original liquid composition. Hence, during boiling or evaporation, the liquid composition, if it changes at all, changes only to a minimal or negligible extent. This is to be contrasted with non-near-azeotrope compositions in which during boiling or evaporation, the liquid composition changes to a substantial degree.

Additionally, near-azeotrope compositions exhibit dew point pressure and bubble point pressure with virtually no pressure differential. That is to say that the difference in the dew point pressure and bubble point pressure at a given temperature will be a small value. It may be stated that compositions with a difference in dew point pressure and bubble point pressure of less than or equal to 3 percent (based upon the bubble point pressure) may be considered to be a near-azeotrope.

Accordingly, the essential features of an azeotrope or a near-azeotrope composition are that at a given pressure, the boiling point of the liquid composition is fixed and that the composition of the vapor above the boiling composition is essentially that of the boiling liquid composition (i.e., no fractionation of the components of the liquid composition takes place). It is also recognized in the art that both the boiling point and the weight percentages of each component of the azeotrope composition may change when the azeotrope or near-azeotrope liquid composition is subjected to boiling at different pressures. Thus, an azeotrope or a near-azeotrope composition may be defined in terms of the unique relationship that exists among the components or in terms of the compositional ranges of the components or in terms of exact weight percentages of each component of the composition characterized by a fixed boiling point at a specified pressure.

It should be understood that while an azeotrope or near-azeotrope composition may exist at a particular ratio of the components at given temperatures and pressures, the azeotrope composition may also exist in compositions containing other components. These additional components include the individual components of the azeotrope composition, said components being present as an excess above the amount being present as the azeotrope composition. For example, the azeotrope of a hydrofluoroolefin and hydrogen fluoride may be present in a composition that has an excess of said hydrofluoroolefin, meaning that the azeotrope composition is present and additional hydrofluoroolefin is also present. Also for example, the azeotrope of a hydrofluoroolefin and hydrogen fluoride as well as an azeotrope of the starting hydrofluorocarbon and hydrogen fluoride may be present in a composition that has an excess of the starting hydrofluorocarbon used for the dehydrofluorination reaction to produce said hydrofluoroolefin, meaning that the azeotrope composition is present and additional starting hydrofluorocarbon is also present. For instance, the azeotrope of HFC-1225ye (CF₃CF═CHF) and hydrogen fluoride may be present in a composition that has an excess of HFC-1225ye, meaning that the azeotrope composition is present and additional HFC-1225ye is also present. Also, for example, the azeotrope of HFC-1225ye (CF₃CF═CHF) and hydrogen fluoride may be present in a composition that has an excess of a suitable starting hydrofluorocarbon for the dehydrofluorination reaction, such as HFC-236ea, meaning that the azeotrope composition is present and additional HFC-236ea is also present.

It has been discovered that both hydrofluoroolefins and hydrofluorocarbons may form azeotrope compositions with hydrogen fluoride. Generally, the hydrofluoroolefin/hydrogen fluoride azeotrope composition will boil at a lower temperature than the corresponding precursor hydrofluorocarbon/hydrogen fluoride azeotrope composition. Thus, it should be possible to separate the hydrofluoroolefin/hydrogen fluoride azeotrope from the hydrofluorocarbon/hydrogen fluoride azeotrope, or to separate the hydrofluoroolefin/hydrogen fluoride azeotrope from the hydrofluorocarbon by azeotropic distillation.

The present process to produce hydrofluoroolefin may further comprise the step of distilling the product mixture to produce a distillate composition comprising an azeotrope composition containing hydrofluoroolefin and hydrogen fluoride.

The distillation step may additionally provide a column bottoms composition comprising unconverted hydrofluorocarbon used in the dehydrofluorination reaction. There may additionally be some amount of hydrogen fluoride present in the column bottoms composition. The amount of hydrogen fluoride in the hydrofluorocarbon from the bottom of the distillation column may vary from about 50 mole percent to less than 1 part per million (ppm, mole basis) depending on the manner in which the dehydrofluorination reaction is conducted.

One embodiment for operating the present distillation involves providing an excess of hydrofluoroolefin to the distillation column. If the proper amount of hydrofluoroolefin is fed to the column, then all the hydrogen fluoride may be taken overhead as an azeotrope composition containing hydrofluoroolefin and hydrogen fluoride. Thus, the hydrofluorocarbon removed from the column bottoms will be essentially free of hydrogen fluoride.

As described herein, by “essentially free of hydrogen fluoride” is meant that the composition contains less than about 100 ppm (mole basis), preferably less than about 10 ppm and most preferably less than about 1 ppm, of hydrogen fluoride.

A further aspect provides a process for the separation of a hydrofluoroolefin from a hydrofluorocarbon wherein said hydrofluoroolefin contains one less fluorine atom and one less hydrogen atom than said hydrofluorocarbon, said process comprising forming a mixture comprising hydrofluoroolefin, hydrofluorocarbon and hydrogen fluoride; and subjecting said mixture to a distillation step forming a column distillate composition comprising an azeotrope or near-azeotrope composition of hydrogen fluoride and hydrofluoroolefin essentially free of said hydrofluorocarbon.

As described herein, by “essentially free of said hydrofluorocarbon” is meant that the composition contains less than about 100 ppm (mole basis), preferably less than about 10 ppm and most preferably less than about 1 ppm, of hydrofluorocarbon.

The present process to separate a hydrofluoroolefin from a hydrofluorocarbon may further form a column bottoms composition comprising hydrofluorocarbon used in the dehydrofluorination reaction. The column bottoms composition comprising hydrofluorocarbon may contain some amount of hydrogen fluoride. The amount of hydrogen fluoride in the hydrofluorocarbon from the bottom of the distillation column may vary from about 50 mole percent to less than 1 part per million (ppm, mole basis) depending on the manner in which the dehydrofluorination reaction is conducted.

One embodiment for operating the present distillation involves providing an excess of hydrofluoroolefin to the distillation column. If the proper amount of hydrofluoroolefin is fed to the column, then all the hydrogen fluoride may be taken overhead as an azeotrope composition containing hydrofluoroolefin and hydrogen fluoride. Thus, the hydrofluorocarbon removed from the column bottoms will be essentially free of hydrogen fluoride.

In the distillation step, the distillate composition exiting the distillation column overhead comprising hydrogen fluoride and hydrofluoroolefin may be condensed using, for example, standard reflux condensers. At least a portion of this condensed stream may be returned to the top of the column as reflux. The ratio of the condensed material, which is returned to the top of the distillation column as reflux, to the material removed as distillate is commonly referred to as the reflux ratio. The specific conditions which may be used for practicing the distillation step depend upon a number of parameters, such as the diameter of the distillation column, feed points, and the number of separation stages in the column, among others. The operating pressure of the distillation column may range from about 10 psi pressure to about 300 psi (1380 kPa), normally about 20 psi to about 75 psi. The distillation column is typically operated at a pressure of about 25 psi (172 kPa). Normally, increasing the reflux ratio results in increased distillate stream purity, but generally the reflux ratio ranges between 0.2/1 to 200/1. The temperature of the condenser, which is located adjacent to the top of the column, is normally sufficient to substantially fully condense the distillate that is exiting from the top of the column, or is that temperature required to achieve the desired reflux ratio by partial condensation.

The column distillate composition comprising an azeotrope or near-azeotrope composition of hydrogen fluoride and hydrofluoroolefin, essentially free of hydrofluorocarbon, may be treated to remove the hydrogen fluoride and provide pure hydrofluoroolefin as product. This may be accomplished, for example, by neutralization. However, the production of substantial amounts of scrubbing discharge can create aqueous waste disposal concerns. Thus, there remains a need for more efficient, economical and environmentally viable processes to remove hydrogen fluoride from this mixture.

It has been discovered that hydrofluoroolefins may be separated from mixtures of hydrofluoroolefins and hydrogen fluoride by a distillation process that takes advantage of changing azeotrope concentrations at different temperatures and pressures.

Another aspect provides a process for the separation of a hydrofluoroolefin from a mixture comprising an azeotrope or near-azeotrope composition of said hydrofluoroolefin and hydrogen fluoride, said process comprising: a) subjecting said mixture to a first distillation step in which a composition enriched in either (i) hydrogen fluoride or (ii) hydrofluoroolefin is removed as a first distillate composition with a first bottoms composition being enriched in the other of said components (i) or (ii); and b) subjecting said first distillate composition to a second distillation step conducted at a different pressure in which the component enriched as first bottoms composition in (a) is removed as a second distillate composition with the bottoms composition of the second distillation step enriched in the same component which was enriched in the first distillate composition.

The first column bottoms composition comprising hydrofluoroolefin may be produced to be essentially free of hydrogen fluoride. Additionally, the second column bottoms sample comprising hydrogen fluoride may be produced to be essentially free of hydrofluoroolefin.

As described herein, by “essentially free of hydrofluoroolefin” is meant that the composition contains less than about 100 ppm (mole basis), preferably less than about 10 ppm and most preferably less than about 1 ppm, of hydrofluoroolefin.

The process as described above takes advantage of the change in azeotrope composition at different pressures to effectuate the separation of hydrofluoroolefin and hydrogen fluoride. The first distillation step may be carried out at high pressure relative to the second distillation step. At higher pressures, the hydrogen fluoride/hydrofluoroolefin azeotrope contains less hydrofluoroolefin. Thus, this high-pressure distillation step produces an excess of hydrofluoroolefin, which boiling at a higher temperature than the azeotrope will exit the column as the column bottoms composition comprising hydrofluoroolefin. The first column distillate composition is then fed to a second distillation step operating at lower pressure. At the lower pressure, the hydrogen fluoride/hydrofluoroolefin azeotrope shifts to lower concentrations of hydrogen fluoride. Therefore, in this second distillation step, there exists an excess of hydrogen fluoride. The excess hydrogen fluoride, having a boiling point higher than the azeotrope, exits the second distillation column as the column bottoms composition comprising hydrogen fluoride.

The reverse of the process described in the preceding paragraph is also possible. The first distillation step may be carried out at a lower pressure relative to the second distillation step. At lower pressure, the hydrogen fluoride/hydrofluoroolefin azeotrope contains less hydrogen fluoride. Thus, this low-pressure distillation step produces an excess of hydrogen fluoride, which boiling at a higher temperature than the azeotrope will exit the column as the bottoms composition comprising hydrogen fluoride. The first column distillate composition is then fed to a second distillation step operating at higher pressure. At the higher pressure, the hydrogen fluoride/hydrofluoroolefin azeotrope shifts to higher concentrations of hydrogen fluoride. Therefore, in this second distillation step, there exists an excess of hydrofluoroolefin. The excess hydrofluoroolefin, having a boiling point higher than the azeotrope, exits the second distillation column as the bottoms composition.

In general, the dehydrofluorination of hydrofluorocarbons is an endothermic reaction and thus may be accomplished in a tubular reactor with catalyst in the tubes and with a heating medium on the shellside of the reactor. Alternatively, a heat carrier may be used to permit adiabatic operation. Either essentially pure hydrofluorocarbon or essentially pure hydrofluoroolefin, both being produced by the distillation processes described herein, may be recycled back to the reactor to serve as heat carrier. Hydrofluorocarbon is a preferred heat carrier, as introduction of hydrofluoroolefin to the dehydrofluorination reactor will result in a reduction in single-pass conversion of hydrofluorocarbon.

In both the first and second distillation steps, the distillate exiting the distillation column overhead comprising hydrogen fluoride and hydrofluoroolefin may be condensed using, for example, standard reflux condensers. At least a portion of this condensed stream may be returned to the top of the column as reflux. The specific conditions which may be used for practicing the distillation steps depend upon a number of parameters, such as the diameter of the distillation column, feed points, and the number of separation stages in the column, among others. The operating pressure of the first distillation column may range from about 50 psi (345 kPa) pressure to about 225 psi (1550 kPa), normally about 50 psi (345 kPa) to about 100 psi (690 kPa). The first distillation column is typically operated at a pressure of about 75 psi (520 kPa). Normally, increasing the reflux ratio results in increased distillate stream purity, but generally the reflux ratio ranges between 0.1/1 to 100/1. The temperature of the condenser, which is located adjacent to the top of the column, is normally sufficient to substantially fully condense the distillate that is exiting from the top of the column, or is that temperature required to achieve the desired reflux ratio by partial condensation.

The operating pressure of the second distillation column may range from about 5 psi (34 kPa) pressure to about 50 psi (345 kPa), normally about 5 psi (34 kPa) to about 20 psi (138 kPa). The second distillation column is typically operated at a pressure of about 17 psi (117 kPa). Normally, increasing the reflux ratio results in increased distillate stream purity, but generally the reflux ratio ranges between 0.1/1 to 50/1. The temperature of the condenser, which is located adjacent to the top of the column, is normally sufficient to substantially fully condense the distillate that is exiting from the top of the column, or is that temperature required to achieve the desired reflux ratio by partial condensation.

FIG. 1 is illustrative of one embodiment for practicing the present two-column distillation process for the separation of hydrofluoroolefin and hydrogen fluoride. Referring to FIG. 1, a feed mixture derived from a prior azeotropic distillation comprising hydrogen fluoride and hydrofluoroolefin, is passed through line (540) to a multiple stage distillation column (510), operating at a temperature of about 77° C. and a pressure of about 335 psi (2310 kPa). The bottoms of the distillation column (510), containing essentially pure hydrofluoroolefin at a temperature of about 86° C. and a pressure of about 337 psi (2320 kPa) is removed from the bottom of column (510) through line (566). The distillate from column (510), containing the hydrogen fluoride/hydrofluoroolefin azeotrope at a temperature of about 77° C. and a pressure of about 335 psi (2310 kPa) is removed from the top of column (510) and sent through line (570) to a multiple stage distillation column (520). The distillate from column (520), containing the hydrogen fluoride/hydrofluoroolefin azeotrope at a temperature of about −19° C. and a pressure of about 17 psi (117 kPa), is removed from column (520) through line (585) and is recycled back to column (510). The bottoms of column (520) containing essentially pure hydrogen fluoride at a temperature of about 26° C. and a pressure of about 19 psi (131 kPa) is removed through line (586).

A further aspect provides a process for the purification of hydrofluoroolefin from a mixture of hydrofluoroolefin, hydrofluorocarbon, and hydrogen fluoride, said process comprising: a) subjecting said mixture to a first distillation step to form a first distillate composition comprising an azeotrope or near-azeotrope composition containing hydrofluoroolefin and hydrogen fluoride and a first bottoms composition comprising hydrofluorocarbon; b) subjecting said first distillate to a second distillation step from which a composition enriched in either (i) hydrogen fluoride or (ii) hydrofluoroolefin is removed as a second distillate composition with a second bottoms composition being enriched in the other of said components (i) or (ii); and c) subjecting said second distillate composition to a third distillation step conducted at a different pressure than the second distillation step in which the component enriched in the second bottoms composition in (b) is removed as a third distillate composition with a third bottoms composition enriched in the same component that was enriched in the second distillate composition.

The present method may optionally further comprise recycling at least some portion of said second bottoms composition (hydrofluoroolefin) to said first distillation step. The recycle of hydrofluoroolefin will ensure that all the hydrogen fluoride is taken overhead as the azeotrope composition with the hydrofluoroolefin. Thus, the hydrofluorocarbon exiting the process as the first column bottoms composition may be produced to be essentially free of hydrogen fluoride and hydrofluoroolefin. The hydrofluoroolefin exiting the process as the second column bottoms composition may be produced to be essentially free of hydrogen fluoride. The hydrogen fluoride exiting the process as the third column bottoms composition may be produced to be essentially free of hydrofluoroolefin.

As described herein, by “essentially free of hydrogen fluoride and hydrofluoroolefin” is meant that the composition contains less than about 100 ppm (mole basis), preferably less than about 10 ppm and most preferably less than about 1 ppm, of each of hydrogen fluoride and hydrofluoroolefin.

The conditions for the first distillation step are the same as those for the azeotropic distillation process for separation of hydrofluoroolefin from hydrofluorocarbon, described earlier herein. The conditions for the second and third distillation steps are the same as the conditions for the 2 column process for separation of hydrofluoroolefin from hydrogen fluoride, also described earlier herein.

A further aspect provides a process to produce hydrofluoroolefin comprising: a) feeding hydrofluorocarbon containing at least one hydrogen and at least one fluorine on adjacent carbons to a reaction zone for dehydrofluorination to form a reaction product composition comprising hydrofluoroolefin, unreacted hydrofluorocarbon and hydrogen fluoride; b) subjecting said reaction product composition to a first distillation step to form a first distillate composition comprising an azeotrope or near-azeotrope composition containing hydrofluoroolefin and hydrogen fluoride and a first bottoms composition comprising hydrofluorocarbon; c) subjecting said first distillate composition to a second distillation step from which a composition enriched in either (i) hydrogen fluoride or (ii) hydrofluoroolefin is removed as a second distillate composition with a second bottoms composition being enriched in the other of said components (i) or (ii); and d) subjecting said second distillate composition to a third distillation step conducted at a different pressure than the second distillation step in which the component enriched in the second bottoms composition in (c) is removed as a third distillate composition with a third bottoms composition enriched in the same component that was enriched in the second distillate composition.

Optionally, the process may further comprise recycling at least some portion of said first bottoms composition (hydrofluorocarbon) to said reaction zone. Optionally, the process may further comprise recycling at least some portion of said second bottoms composition or said third bottoms composition (i.e. that which is hydrofluoroolefin) to said reaction zone. Optionally, the process may further comprise recycling at least some portion of said second bottoms composition or said third bottoms composition (i.e. that which is hydrofluoroolefin) to said first distillation step. Optionally, the process may further comprise recovering at least some portion of said second bottoms composition or said third bottoms composition as hydrofluoroolefin essentially free of hydrofluorocarbon and hydrogen fluoride.

As described herein, by “essentially free of hydrofluorocarbon and hydrogen fluoride” is meant that the composition contains less than about 100 ppm (mole basis), preferably less than about 10 ppm and most preferably less than about 1 ppm, of each of hydrofluorocarbon and hydrogen fluoride.

FIG. 2 is illustrative of one embodiment for practicing the present process for production of hydrofluoroolefin. Hydrofluorocarbon is fed through line (360) to reactor (320). The reactor effluent mixture comprising hydrogen fluoride, hydrofluorocarbon and hydrofluoroolefin, exits the reactor through line (450) and is fed to a multiple stage distillation column (410). The bottoms of distillation column (410), containing essentially pure hydrofluorocarbon is removed from the bottom of column (410) through line (466) and may be recycled back to the reactor. The distillate from column (410), containing the hydrogen fluoride/hydrofluoroolefin azeotrope is removed from the top of column (410) and is sent through line (540) to a second multiple stage distillation column (510). The bottoms from column (510), which is essentially pure hydrofluoroolefin, is removed from column (510) through line (566) and may be recycled back to the reactor (320) as a heat carrier. The distillate from column (510), containing the hydrogen fluoride/hydrofluoroolefin azeotrope, is fed through line (570) to a third multiple stage distillation column (520). The distillate from column (520) comprising hydrogen fluoride/hydrofluoroolefin is removed through line (585) and may be recycled to the second distillation column (510). The bottoms composition from column (520) is essentially pure hydrogen fluoride and is removed from column (520) through line (586). The essentially pure hydrogen fluoride product from this process may be used in any manner appropriate such as feeding to a fluorination reactor for production of a fluorochemical compound, or may be neutralized for disposal.

While not illustrated in the Figures, it is understood that certain pieces of process equipment may be used in the processes described herein, for optimization. For instance, pumps, heaters or coolers may be used where appropriate. As an example, it is desirable to have the feed to a distillation column at the same temperature as the point in the column that it is fed. Therefore, heating or cooling of the process stream may be necessary to match the temperature.

Another embodiment provides a process of producing CF₃CH═CF₂ by pyrolysis of CF₃CH₂CF₃. The process may be written as:

CF₃CH₂CF₃+Δ→CF₃CH═CF₂+HF

where Δ represents heat and HF is hydrogen fluoride.

Pyrolysis, as the term is used herein, means chemical change produced by heating in the absence of catalyst. Pyrolysis reactors generally comprise three zones: a) a preheat zone, in which reactants are brought close to the reaction temperature; b) a reaction zone, in which reactants reach reaction temperature and are at least partially pyrolyzed, and products and any byproducts form; c) a quench zone, in which the stream exiting the reaction zone is cooled to stop the pyrolysis reaction. Laboratory-scale reactors have a reaction zone, but the preheating and quenching zones may be omitted.

In this embodiment, the reactor may be of any shape consistent with the process but is preferably a cylindrical tube, either straight or coiled. Although not critical, such reactors typically have an inner diameter of from about 1.3 to about 5.1 cm (about 0.5 to about 2 inches). Heat is applied to the outside of the tube, the chemical reaction taking place on the inside of the tube. The reactor and its associated feed lines, effluent lines and associated units should be constructed, at least as regards the surfaces exposed to the reaction reactants and products, of materials resistant to hydrogen fluoride. Typical materials of construction, well-known to the fluorination art, include stainless steels, in particular of the austenitic type, the well-known high nickel alloys, such as Monel® nickel-copper alloys, Hastelloy-based alloys and Inconel® nickel-chromium alloys and copper clad steel. Where the reactor is exposed to high temperature the reactor may be constructed of more than one material. For example, the outer surface layer of the reactor should be chosen for ability to maintain structural integrity and resist corrosion at the pyrolysis temperature, the inner surface layer of the reactor should be chosen of materials resistant to attack by, that is, inert to, the reactant and products. In the case of the present process, the product hydrogen fluoride is corrosive to certain materials. In other words, the reactor may be constructed of an outer material chosen for physical strength at high temperature and an inner material chosen for resistance to corrosion by the reactants and products under the temperature of the pyrolysis.

For the process of this embodiment, it is preferred that the reactor inner surface layer be made of high nickel alloy, that is an alloy containing at least about 50 wt % nickel, preferably a nickel alloy having at least about 75 wt % nickel, more preferably a nickel alloy having less than about 8 wt % chromium, still more preferably a nickel alloy having at least about 98 wt % nickel, and most preferably substantially pure nickel, such as the commercial grade known as Nickel 200. More preferable than nickel or its alloys as the material for the inner surface layer of the reactor is gold. The thickness of the inner surface layer does not substantially affect the pyrolysis and is not critical so long as the integrity of the inner surface layer is intact. The thickness of the inner surface layer is typically from about 10 to about 100 mils (0.25 to 2.5 mm). The thickness of the inner surface layer can be determined by the method of fabrication, the cost of materials, and the desired reactor life.

The reactor outer surface layer is resistant to oxidation or other corrosion and maintains sufficient strength at the reaction temperatures to keep the reaction vessel from failing of distorting. This layer is preferably Inconel® alloy, more preferably Inconel® 600.

The present pyrolysis of CF₃CH₂CF₃ to CF₂═CHCF₃ and HF is carried out in the absence of catalyst in a substantially empty reactor. By absence of catalyst is meant that no material or treatment is added to the pyrolysis reactor that increases the reaction rate by reducing the activation energy of the pyrolysis process. It is understood that although surfaces that are unavoidably present in any containment vessel, such as a pyrolysis reactor, may have incidental catalytic or anticatalytic effects on the pyrolysis process, the effect makes an insignificant contribution, if any, to the pyrolysis rate. More specifically, absence of catalyst means absence of conventional catalysts having high surface area in a particulate, pellet, fibrous or supported form that are useful in promoting the elimination of hydrogen fluoride from a hydrofluorocarbon (i.e., dehydrofluorination). Example, dehydrofluorination catalysts include: chromium oxide, optionally containing other metals, metal oxides or metal halides; chromium fluoride, unsupported or supported; and activated carbon, optionally containing other metals, metal oxides or metal halides.

Substantially empty reactors useful for carrying out the present process are tubes comprising the aforementioned materials of construction. Substantially empty reactors include those wherein the flow of gases through the reactor is partially obstructed to cause back-mixing, i.e. turbulence, and thereby promote mixing of gases and good heat transfer. This partial obstruction can be conveniently obtained by placing packing within the interior of the reactor, filling its cross-section or by using perforated baffles. The reactor packing can be particulate or fibrillar, preferably in cartridge disposition for ease of insertion and removal, has an open structure like that of Raschig Rings or other packings with a high free volume, to avoid the accumulation of coke and to minimize pressure drop, and permits the free flow of gas. Preferably the exterior surface of such reactor packing comprises materials identical to those of the reactor inner surface layer; materials that do not catalyze dehydrofluorination of hydrofluorocarbons and are resistant to hydrogen fluoride. The free volume is the volume of the reaction zone minus the volume of the material that makes up the reactor packing. The free volume is at least about 80%, preferably at least about 90%, and more preferably about 95%.

The pyrolysis which accomplishes the conversion of CF₃CH₂CF₃ to CF₂═CHCF₃ is suitably conducted at a temperature of at least about 700° C., preferably at least about 750° C., and more preferably at least about 800° C. The maximum temperature is no greater than about 1,000° C., preferably no greater than about 950° C., and more preferably no greater than about 900° C. The pyrolysis temperature is the temperature of the gases inside at about the mid-point of the reaction zone.

The residence time of gases in the reaction zone is typically from about 0.5 to about 60 seconds, more preferably from about 2 seconds to about 20 seconds at temperatures of from about 700 to about 900° C. and atmospheric pressure. Residence time is determined from the net volume of the reaction zone and the volumetric feed rate of the gaseous feed to the reactor at a given reaction temperature and pressure, and refers to the average amount of time a volume of gas remains in the reaction zone.

The pyrolysis is preferably carried out to a conversion of the CF₃CH₂CF₃ at least about 25%, more preferably to at least about 35%, and most preferably to at least about 45%. By conversion is meant the portion of the reactant that is consumed during a single pass through the reactor. Pyrolysis is preferably carried out to a yield of CF₃CH═CF₂ of at least about 50%, more preferably at least about 60%, and most preferably at least about 75%. By yield is meant the moles of CF₃CH═CF₂ produced per mole of CF₃CH₂CF₃ consumed.

The reaction is preferably conducted at subatmospheric, or atmospheric total pressure. That is, the reactants plus other ingredients are at subatmospheric pressure or atmospheric pressure. (If inert gases are present as other ingredients, as discussed below, the sum of the partial pressures of the reactants plus such ingredients is subatmospheric or atmospheric). Near atmospheric total pressure is more preferred. The reaction can be beneficially run under reduced total pressure (i.e., total pressure less than one atmosphere).

The reaction according to this embodiment can be conducted in the presence of one or more unreactive diluent gases, that is diluent gases that do not react under the pyrolysis conditions. Such unreactive diluent gases include the inert gases nitrogen, argon, and helium. Fluorocarbons that are stable under the pyrolysis conditions, for example, trifluoromethane and perfluorocarbons, may also be used as unreactive diluent gases. It has been found that inert gases can be used to increase the conversion of CF₃CH₂CF₃ to CF₃CH═CF₂. Of note are processes where the mole ratio of inert gas to CF₃CH₂CF₃ fed to the pyrolysis reactor is from about 5:1 to 1:1. Nitrogen is a preferred inert gas because of its comparatively low cost.

The present process produces a 1:1 molar mixture of HF and CF₃CH═CF₂ in the reactor exit stream. The reactor exit stream can also contain unconverted reactant, CF₃CH₂CF₃. The components of the reactor exit stream can be separated by conventional means, such as distillation. Hydrogen fluoride and CF₃CH═CF₂ form a homogenous low-boiling azeotrope containing about 60 mole percent CF₃CH═CF₂. The present process reactor exit stream can be distilled and the low-boiling HF and CF₃CH═CF₂ azeotrope taken off as a distillation column overhead stream, leaving substantially pure CF₃CH₂CF₃ as a distillation column bottom stream. Recovered CF₃CH₂CF₃ reactant may be recycled to the reactor. CF₃CH═CF₂ can be separated from its azeotrope with HF by conventional procedures, such as pressure swing distillation or by neutralization of the HF with caustic.

Without further elaboration, it is believed that one skilled in the art can, using the description herein, utilize the disclosed compositions and processes to their fullest extent. The following exemplary embodiments are, therefore, to be construed as merely illustrative, and do not constrain the remainder of the disclosure in any way whatsoever.

EXAMPLES Example 1 Dehydrofluorination of CF₃CH₂CHF₂ to CF₃CH═CHF (E and Z Isomers Over Carbonaceous Catalyst

A Hastelloy™ nickel alloy reactor (2.54 cm OD×2.17 cm ID×24.1 cm L) was charged with 14.32 g (25 mL) of spherical (8 mesh) three dimensional matrix porous carbonaceous material prepared substantially as described in U.S. Pat. No. 4,978,649, incorporated herein by reference. The packed portion of the reactor was heated by a 5″×1″ ceramic band heater clamped to the outside of the reactor. A thermocouple positioned between the reactor wall and the heater measured the reactor temperature. After charging the reactor with the carbonaceous material, nitrogen (10 ml/min, 1.7×10⁻⁷ m³/s) was passed through the reactor and the temperature was raised to 200° C. during a period of one hour and maintained at this temperature for an additional 4 hours. The reactor temperature was then raised to the desired operating temperature and a flow of CF₃CH₂CHF₂ and nitrogen was started through the reactor.

A portion of the total reactor effluent was sampled on-line for organic product analysis using a gas chromatograph equipped with a mass selective detector (GC-MS); the results are summarized in Table 3. The bulk of the reactor effluent containing organic products and also inorganic acid, such as HF, was treated with aqueous caustic for neutralization.

TABLE 3 Reactor CF₃CH₂CHF₂ GC Area Percent Temp. feed N₂ feed E- Z- (° C.) (mL/min) (mL/min) CF₃CH═CHF CF₃CH═CHF CF₃CH₂CHF₂ Unks 200 10 20 0.1 ND 99.6 0.3 250 10 20 0.8 ND 99.0 0.2 300 10 20 8.9 ND 90.9 0.2 350 10 10 31.6 5.7 62.3 0.4 350 10 5 42.4 8.7 48.3 0.6 ND = not detected

Example 2 Dehydrofluorination of CF₃CH₂CHF₂ to CF₃CH═CHF (E and Z Isomers Over Fluorided Alumina Catalyst

A 15 in (38.1 cm)×⅜ in (0.95 cm) Hastelloy tube was charged with 7.96 grams (13 cc) of gamma-alumina ground to 12-20 mesh (0.84 to 1.68 mm). The catalyst was activated by heating at 200° C. for 15 minutes under a nitrogen purge (50 sccm, 8.3×10⁻⁷ m³/s). The temperature was raised to 325° C. for 10 minutes, to 400° C. for 20 minutes, and then lowered to 300° C. for 60 minutes. The nitrogen flow was reduced to 35 sccm (5.8×10⁻⁷ m³/s) and anhydrous HF vapor was fed at 12 sccm (2.0×10⁻⁷ m³/s) for 35 minutes. The temperature was then raised to 325° C. for 60 minutes, to 350° C. for 60 minutes, to 375° C. for 90 minutes, to 400° C. for 30 minutes, and to 425° C. for 40 minutes. The nitrogen flow was then reduced to 25 sccm (4.2×10⁻⁷ m³/s) and the HF raised to 20 sccm (3.3×10⁻⁷ m³/s) for 20 minutes. The nitrogen flow was then reduced to 15 sccm (2.5×10⁻⁷ m³/s) and the HF flow increased to 28 sccm (4.7×10⁻⁷ m³/s) for 20 minutes. The nitrogen flow was then reduced to 5 sccm (8.3×10⁻⁸ m³/s) and the HF increased to 36 sccm (6.0×10⁻⁷ m³/s) for 20 minutes. The nitrogen flow was then shut off, and the HF flow increased to 40 sccm (6.7×10⁻⁷ m³/s) for 121 minutes.

The temperature of the reactor was set to 375° C., and CF₃CH₂CHF₂ was fed at a flow rate of 5.46 mL/hour (20.80 sccm, 3.5×10⁻⁷ m³) and nitrogen co-fed at a flow rate of 5.2 sccm (8.7×10⁻⁸ m³). The effluent was analyzed by GC; the results are summarized in Table 4.

TABLE 4 Component GC Area % E—CF₃CH═CHF 71.4 CF₃CH₂CHF₂ 15.2 Z—CF₃CH═CHF 12.1 unknown 1.3

Example 3 Dehdrofluorination of CF₃CHFCHF₂ to CF₃CF═CHF (E and Z Isomers) Over Carbonaceous Catalyst

A mixture of CF₃CHFCHF₂ and nitrogen were passed through the reactor following the procedure of Example 1. The results of GC analysis of the reactor effluent are summarized in Table 5.

TABLE 5 Reactor CF₃CHFCHF₂ GC Area Percent Temp. feed N₂ feed Z- E- (° C.) (mL/min) (mL/min) CF₃CF═CHF CF₃CF═CHF CF₃CHFCHF₂ Unks 200 10 20 0.03 ND 99.97 ND 250 10 20 0.2 0.03 99.8 ND 300 10 20 1.4 0.22 98.4 0.01 350 10 20 5.4 0.96 93.1 0.5 400 10 20 38.1 9.0 51.7 1.1 400 10 10 37.9 8.7 51.6 1.8 400 10 5 42.6 9.5 46.7 1.2 400 10 40 13.2 2.5 71.6 12.7 ND = not detected Unks = unknowns

Example 4 Synthesis of CF₃CF═CH₂ by Dehydrofluorination with Fluorided Alumina Catalyst

A HasteHoy™ tube reactor (2.54 cm OD×2.17 cm ID×24.1 cm L) was filled with 25 cc of gamma-alumina ground to 12-20 mesh (0.84 to 1.68 mm). The catalyst was activated by heating at 200° C. for 15 minutes under a nitrogen purge and then reacted with a HF/N₂ mixture heated up to 425° C. to yield 16.7 gm of activated fluorided alumina.

At a temperature of 350° C., 10 sccm of nitrogen (1.7×10⁻⁷ m³/s) and 15 sccm (2.5×10⁻⁷ m³/s) of CF₃CF₂CH₃ were mixed and flowed through the reactor. The temperature was then raised to 400° C., the flow rates held constant. The effluent for both temperatures was sampled and analyzed by ¹⁹F NMR. Additionally, the effluent was analyzed by GC to determine concentrations as listed in Table 6.

TABLE 6 CF₃CF₂CH₃ Temp., N₂ flow flow Concentrations, (Mole %) ° C. (sccm) (sccm) CF₃CF═CH₂ CF₃CF₂CH₃ Unks 350 10 15 84.2 12.8 3.0 400 10 15 91.3 1.9 6.8 Unks = unknowns

Example 5 Synthesis of CF₃CF═CH₂ with Carbon Catalyst

Following the procedure of Example 3, a mixture of 10 sccm (1.7×10⁻⁷ m³/s) of nitrogen and 15 sccm (2.5×10⁻⁷ m³/s) of CF₃CF₂CH₃ were passed through the reactor giving a contact time of 60 seconds. The flows were reduced to 5 sccm 8.3×10⁻⁸ m³/s) of nitrogen (and 7.5 sccm (1.3×10⁻⁷ m³/s) of CF₃CF₂CH₃ giving a contact time of 120 seconds. The effluent was sampled under both sets of conditions and analyzed by ¹⁹F NMR. The effluent compositions as determined by GC are listed in Table 7.

TABLE 7 CF₃CF₂CH₃ Temp., N₂ flow flow Concentrations, Mole % ° C. (sccm) (sccm) CF₃CF═CH₂ CF₃CF₂CH₃ Unks 400 10 15 6.0 93.9 0.1 400 5 7.5 22.8 76.4 0.8 Unks = unknowns

Example 6 Synthesis of CHF₂CF═CHF from CHF₂CF₂CH₂F

A 0.375 inch (0.95 cm) O.D. Hastelloy™ nickel alloy tube was charged with 7.0 grams (10 cc) of gamma-alumina ground to 12/20 mesh (0.84 to 1.68 mm). The tube was purged with nitrogen (50 sccm, 8.3×10⁻⁷ m³/s) for twenty minutes as the temperature was raised from 40° C. to 175° C. The nitrogen flow was continued as anhydrous hydrogen fluoride (50 sccm, 8.3×10⁻⁷ m³/s) was added to the reactor for about 1.5 hours. The nitrogen flow was then reduced to 20 sccm (3.3×10⁻⁷ m³/s) and the hydrogen fluoride flow increased to 80 sccm (1.3×10⁻⁶ m³/s) as the temperature in the tube was increased from 174° C. to 373° C. over the course of 3.7 hours. The nitrogen flow was then reduced to 10 sccm (1.7×10⁻⁷ m³/s) and the hydrogen fluoride flow was maintained at 80 sccm (1.3×10⁻⁶ m³/s) for one hour at 400° C. The reactor temperature was then adjusted to 290° C. and the reactor purged with nitrogen.

CHF₂CF₂CH₂F was vaporized and fed to the reactor at such a rate as to maintain a contact time with the catalyst of 120 seconds. No nitrogen co-feed was present. Gas chromatographic analyses of the reactor effluent at three temperatures are listed in Table 8.

TABLE 8 GC Area Percent Reactor E and Temp, ° C. CHF₂CF₂CH₂F CHF₂CHFCHF₂ Z—CHF₂CF═CHF 275 72.3 5.5 22.0 325 40.8 6.9 51.7 375 27.0 3.2 68.9

Example 7 Synthesis of CF₃CH═CFCF₃

A Hastelloy™ nickel alloy reactor (2.54 cm OD×2.17 cm ID×24.1 cm L) was charged with 13.5 g (25 mL) of spherical (8 mesh) three dimensional matrix porous carbonaceous material, as described in Example 1.

Ata temperature of 300° C., 12.5 sccm of nitrogen (2.1×10⁻⁷ m³/s) and 12.5 sccm (2.1×10⁻⁷ m³/s) of CF₃CHFCHFCH₃ were mixed and flowed through the reactor. The reactor temperature was raised to 350° C. and finally to 400° C. and the effluent were analyzed by GC/MS at each temperature. The effluent composition is listed in Table 9.

TABLE 9 Reactor Mole percent Temp., E— and ° C. CF₃CF═CFCF₃ Z—CF₃CH═CFCF₃ CF₃CHFCHFCF₃ CF₃C≡CCF₃ unknowns 300 0.2 24.4 73.3 ND 2.1 350 0.2 71.6 26.1 ND 2.1 400 — 90.1 8.3 0.4 1.2

Example 8 Synthesis of CH₂═CFCH₂CF₃ and E/Z—CF₃CH═CFCH₃

A Hastelloy™ nickel alloy reactor (2.54 cm OD×2.17 cm ID×24.1 cm L) was charged with 13.5 g (25 mL) of spherical (8 mesh) three dimensional matrix porous carbonaceous material, as described in Example 1.

At a temperature of 350° C., 25 sccm of N₂ (4.2×10⁻⁷ m³/s) and 25 sccm (4.2×10⁻⁷ m³/s) of CF₃CH₂CF₂CH₃ were mixed and flowed through the reactor. The effluent was analyzed by GC/MS and the results are listed in Table 10.

TABLE 10 Component Mole Percent CH₂═CFCH₂CF₃ 14.5 E—and Z—CF₃CH═CFCH₃ 11.9 CF₃CH₂CF₂CH₃ 72.0 unknowns 1.6

Example 9 Dehdrofluorination of CF₃CHFCHFCF₂CF₃ to CF₃CH═CFCF₂CF₃ and CF₃CF═CHCF₂CF₃ Over Carbonaceous Catalyst

Following the procedure of Example 3, a mixture of nitrogen (10 mL/min, 1.7×10⁻⁷ m³/s) and CF₃CHFCHFCF₂CF₃ (5 mL of liquid/hour) was passed through the reactor. GC analyses of the reactor effluent at several conditions are summarized in Table 11. In Table 11, temp is temperature, unks is unknowns, and other HFCs include CHF₃, CF₃CHF₂, and CF₃CH₂F.

TABLE 11 Reactor N₂ GC Area Percent temp, flow, Z- Z- Other Other Other ° C. sccm Unks CF₃CF═CHCF₂CF₃ CF₃CH═CFCF₂CF₃ C₅HF₉s CF₃CHFCHFCF₂CF₃ C₅H₂F₁₀s HFCs 200 20 1.47 12.9 29.6 0.36 55.0 0.65 0.08 200 20 2.05 10.7 24.3 0.29 62.1 0.47 0.09 250 20 2.24 28.1 59.6 1.30 1.01 7.43 0.09 250 20 2.07 28.1 59.9 1.30 1.00 7.35 0.33 250 40 2.14 28.9 60.2 1.35 0.90 6.25 0.32

Example 10 Phase Studies of Mixtures of HF and E-CF₃CH═CHF

A phase study was performed for a composition consisting essentially of E-CF₃CH═CHF and HF, wherein the composition was varied and the vapor pressures were measured at both 20° C. and 70° C. Based upon the data from the phase studies, azeotropic compositions at other temperature and pressures have been calculated.

Table 12 provides a compilation of experimental and calculated azeotropic compositions for HF and E-CF₃CH═CHF at specified temperatures and pressures.

TABLE 12 Temperature, Pressure, Mole % ° C. psi (kPA) Mole % HF E—CF₃CH═CHF −20 15.5 (107)   27.3 72.7 0 35.6 (242)   29.7 70.3 20 70.4 (485)   30.7 69.3 40 127 (878)  31.5 68.5 60 215 (1482) 31.6 68.4 65 242 (1669) 31.5 68.5 70 273 (1881) 31.4 68.6 75 307 (2117) 31.2 68.8 80 345 (2376) 31.0 69.0 85 386 (2661) 30.7 69.3 90 431 (2972) 30.4 69.6 95 482 (3323) 30.0 70.0 100 539 (3715) 29.5 70.5

Example 11 Phase Studies of Mixtures of HF and Z—CF₃CF═CHF

A phase study was performed for a composition consisting essentially of Z—CF₃CF═CHF and HF, wherein the composition was varied and the vapor pressures were measured at both 19.5° C. and 70° C. Based upon the data from the phase studies, azeotrope compositions at other temperature and pressures have been calculated.

Table 13 provides a compilation of experimental and calculated azeotrope compositions for HF and Z—CF₃CF═CHF at specified temperatures and pressures.

TABLE 13 Temperature, Pressure, Mole % Mole % ° C. psi (kPa) HF Z—CF₃CF═CHF −25 12.8 (88.3)  31.0 69.0 −20 16.7 (115)   31.7 68.3 −10 24.7 (170)   32.6 67.4 0 36.5 (252)   33.4 66.6 19.5 72.1 (497)   34.4 65.6 25 85.8 (592)   34.5 65.5 50 175 (1208) 35.0 65.0 75 323 (2226) 35.2 64.8 77 335 (2308) 35.2 64.8 80 361 (2490) 35.3 64.7 85 403 (2777) 35.3 64.7 90 448 (3090) 35.4 64.6 95 497 (3429) 35.4 64.6 100 551 (3799) 35.5 64.5

Example 12 Phase Studies of Mixtures of HF and a Mixture of Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃

A phase study was performed for a composition consisting essentially of a mixture of Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃ and HF, wherein the composition was varied and the vapor pressures were measured at both 20° C. and 70° C. Based upon the data from the phase studies, azeotrope compositions at other temperature and pressures have been calculated.

Table 14 provides a compilation of experimental and calculated azeotrope compositions for HF and a mixture of Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃ at specified temperatures and pressures.

TABLE 14 Mole % Temperature, Pressure, Mole % Z—CF₃CH═CFCF₂CF₃ and ° C. psi (kPa) HF Z—CF₃CF═CHCF₂CF₃ −20 4.1 (28.3) 88.6 11.4 −15 5.3 (36.5) 87.8 12.2 −10 6.7 (46.2) 87.0 13.0 −5 8.5 (58.6) 86.2 13.8 0 10.6 (73.1)  85.3 14.7 20 24.2 (167)   82.0 18.0 40 49.3 (340)   78.6 21.4 60 92.8 (639)   75.1 24.9 65 108 (742)  74.2 25.8 70 124 (855)  73.4 26.6 75 143 (988)  72.5 27.5 80 165 (1136) 71.6 28.4 85 189 (1300) 70.6 29.4 90 217 (1495) 69.7 30.3 95 248 (1713) 68.6 31.4 100 285 (1965) 67.4 32.6

Example 13 Phase Studies of Mixtures of HF and CF₃CHFCHFCF₂CF₃

A phase study was performed for a composition consisting essentially of CF₃CHFCHFCF₂CF₃ and HF, wherein the composition was varied and the vapor pressures were measured at both 30° C. and 80° C. Based upon the data from the phase studies, azeotrope compositions at other temperature and pressures have been calculated.

Table 15 provides a compilation of experimental and calculated azeotrope compositions for HF and CF₃CHFCHFCF₂CF₃ at specified temperatures and pressures.

TABLE 15 Temperature, Pressure, Mole % ° C. psi (kPa) Mole % HF CF₃CHFCHFCF₂CF₃ −20   3.0 (20.7) 97.3 2.7 0   7.7 (53.1) 95.5 4.5 20 17.3 (119) 93.2 6.8 30 25.0 (172) 91.9 8.1 39.5 34.7 (239) 90.7 9.3 40 35.3 (243) 90.6 9.4 60 66.6 (459) 87.8 12.2 65 77.3 (533) 87.0 13.0 70 89.3 (616) 86.3 13.7 75  103 (710) 85.5 14.5 80  118 (814) 84.8 15.2 85  135 (931) 84.0 16.0 90   154 (1062) 83.3 16.7 95   175 (1207) 82.6 72.4 97.2   185 (1276) 82.2 17.8 100   198 (1365) 81.8 18.2

Example 14 Phase Studies of Mixtures of HF and CF₃CF═CH₂

A phase study was performed for a composition consisting essentially of CF₃CF═CH₂ and HF, wherein the composition was varied and the vapor pressures were measured at both 9.3° C. and 44.4° C. Based upon the data from the phase studies, azeotrope compositions at other temperature and pressures have been calculated.

Table 16 provides a compilation of experimental and calculated azeotrope compositions for HF and CF₃CF═CH₂ at specified temperatures and pressures.

TABLE 16 Temperature, Pressure, Mole % ° C. psi (kPa) Mole % HF CF₃CF═CH₂ −20 23.2 (160)   19.3 80.7 −18.5 24.7 (170)   19.7 80.3 0 49.5 (341)   23.0 77.0 9.3 67.6 (466)   24.4 75.6 20 94.6 (652)   25.7 74.3 40 167 (1151) 27.7 72.3 44.4 187 (1289) 28.0 72.0 60 278 (1917) 29.5 70.5 70 354 (2441) 30.3 69.7 71.2 365 (2517) 30.4 69.6 75 400 (2758) 30.7 69.3 80 453 (3123) 31.1 68.9

Example 15 Phase Studies of Mixtures of HF and CF₃CH═CF₂

A phase study was performed for a composition consisting essentially of CF₃CH═CF₂ and HF, wherein the composition was varied and the vapor pressures were measured at both 0.3° C. and 50.1° C. Based upon the data from the phase studies, azeotrope compositions at other temperature and pressures have been calculated.

Table 17 provides a compilation of experimental and calculated azeotrope compositions for HF and CF₃CH═CF₂ at specified temperatures and pressures.

TABLE 17 Temperature, Pressure, Mole Mole % ° C. psi (kPa) % HF CF₃CH═CF₂ −20 17.4 (120)   29.6 70.4 −17 19.7 (136)   29.9 70.1 −3 34.7 (239)   31.0 69.0 0 38.8 (267)   30.9 69.1 0.3 39.2 (270)   30.9 69.1 3.9 44.7 (308)   31.0 69.0 20 76.7 (529)   32.8 67.2 40 139 (958)  34.0 66.0 50.1 183 (1262) 34.5 65.5 60 236 (1627) 34.9 65.1 65 268 (1848) 35.1 64.9 70 304 (2096) 35.3 64.7 71.5 314.7 (2170)   35.4 64.6 75 344 (2372) 35.6 64.4 80 389 (2682) 35.3 64.7 85 441 (3041) 36.0 64.0 90 524 (3613) 36.9 63.1 95 629 (4337) 37.4 62.6 100 745 (5137) 38.0 62.0

Example 16 Phase Studies of Mixtures of HF and a Mixture of Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅

A phase study was performed for a composition consisting essentially of HF and a mixture of Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅, wherein the composition was varied and the vapor pressures were measured at both 19.9° C. and 69.6° C. Based upon the data from the phase studies, azeotrope compositions at other temperature and pressures have been calculated.

Table 18 provides a compilation of experimental and calculated azeotrope compositions for HF and a mixture of Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅ at specified temperatures and pressures.

TABLE 18 Mole % Temperature, Pressure, Mole % Z—C₂F₅CF═CHCF₂C₂F₅ ° C. psi (kPa) HF and Z—C₂F₅CH═CFCF₂C₂F₅ −20   2.9 (20.0) 98.7 1.3 −15   3.7 (25.5) 98.5 1.5 −10   4.7 (32.4) 98.3 1.7 −5   5.9 (40.7) 98.1 1.9 0   7.3 (50.3) 97.9 2.1 19.9 16.3 (112) 96.7 3.3 20 16.3 (112) 96.7 3.3 25.1 19.7 (136) 96.4 3.6 40 33.2 (229) 95.4 4.6 60 62.3 (430) 93.9 6.1 65 72.1 (497) 93.5 6.5 69.6 82.2 (567) 93.1 6.9 70 83.3 (574) 93.1 6.9 75 95.7 (660) 92.7 7.3 80  110 (758) 92.3 7.7 85  125 (862) 91.9 8.1 90  143 (986) 91.5 8.5 95   162 (1117) 91.2 8.8 100   183 (1262) 90.8 9.2 108.4   225 (1551) 90.3 9.7

Example 17 Phase Studies of Mixtures of HF and C₂F₅CHFCHFCF₂C₂F₅

A phase study was performed for a composition consisting essentially of C₂F₅CHFCHFCF₂C₂F₅ and HF, wherein the composition was varied and the vapor pressures were measured at both 30.8° C. and 80.2° C. Based upon the data from the phase studies, azeotrope compositions at other temperature and pressures have been calculated.

Table 19 provides a compilation of experimental and calculated azeotrope compositions for HF and C₂F₅CHFCHFCF₂C₂F₅ at specified temperatures and pressures.

TABLE 19 Temperature, Pressure, Mole % ° C. psi (kPa) Mole % HF C₂F₅CHFCHFCF₂C₂F₅ 13.5  11.9 (82.0) <100 0.003 14  12.1 (83.4) 99.9 0.1 14.5  12.3 (84.8) 99.9 0.1 15  12.6 (86.9) 99.8 0.2 20 15.1 (104) 99.3 0.7 25 18.1 (125) 98.8 1.2 27.4 19.7 (136) 98.6 1.4 30 21.6 (149) 98.5 1.5 30.8 22.2 (153) 98.5 1.5 40 30.3 (209) 98.2 1.8 50 41.7 (288) 97.7 2.3 60 56.5 (390) 97.3 2.7 70 75.3 (519) 96.8 3.2 80 99.1 (683) 96.3 3.7 80.2 99.6 (687) 96.3 3.7 90  129 (889) 95.8 4.2 99.8   165 (1138) 95.4 4.6 100   165 (1138) 95.4 4.6 110   210 (1484) 95.0 5.0 120   264 (1820) 94.7 5.3

Example 18 Azeotropic Distillation for Separation of E-CF₃CH═CHF from CF₃CH₂CHF₂

A mixture of HF, E-CF₃CH═CHF, and CF₃CH₂CHF₂ is fed to a distillation column for the purpose of purification of the E-CF₃CH═CHF. The data in Table 20 were obtained by calculation using measured and calculated thermodynamic properties.

TABLE 20 Component or Column overhead variable Column feed (distillate) Column bottoms CF₃CH₂CHF₂, 17.6 0.7 ppm 100 mol % E—CF₃CH═CHF, 76.5 92.9 3 ppm mol % HF, mol %  5.9 7.1 — Temp, ° C. — −6.8   31.1 Pressure, psi — 24.7 (170) 26.7 (184) (kPa)

Example 19 Azeotropic Distillation for Separation of Z—CF₃CF═CHF from CF₃CHFCHF₂

A mixture of HF, Z—CF₃CF═CHF, and CF₃CHFCHF₂ is fed to a distillation column for the purpose of purification of the Z—CF₃CF═CHF. The data in Table 21 were obtained by calculation using measured and calculated thermodynamic properties.

TABLE 21 Component or Column Column overhead variable feed (distillate) Column bottoms CF₃CHFCHF₂, 24.4 1 ppm 99.99 mol % Z—CF₃CF═CHF, 51.2 67.7 68 ppm mol % HF, mol % 24.4 32.3 trace Temp, ° C. — −8.3 21.8  Pressure, psi — 24.7 (170) 26.7 (184) (kPa)

Example 20 Azeotropic Distillation for Separation of Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃ from CF₃CHFCHFCF₂CF₃

A mixture of HF, Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃, and CF₃CHFCHFCF₂CF₃ is fed to a distillation column for the purpose of purification of Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃. The data in Table 22 were obtained by calculation using measured and calculated thermodynamic properties.

TABLE 22 Component or Column Column overhead variable feed (distillate) Column bottoms CF₃CHFCHFCF₂CF₃, 33.4 1 ppm 100 mol % Z—CF₃CH═CFCF₂CF₃ 33.3 50.0 2 ppm and Z—CF₃CF═CHCF₂CF₃, mol % HF, mol % 33.3 50.0 — Temp, ° C. — 30.0   21.8 Pressure, psi (kPa) — 19.7 (136) 21.7 (150)

Example 21 Azeotropic Distillation for Separation of CF₃CF═CH₂ from CF₃CF₂CH₃

A mixture of HF, CF₃CF═CH₂, and CF₃CF₂CH₃ is fed to a distillation column for the purpose of purification of CF₃CF═CH₂. The data in Table 23 were obtained by calculation using measured and calculated thermodynamic properties.

TABLE 23 Component or Column overhead variable Column feed (distillate) Column bottoms CF₃CF₂CH₃, 27.3 10 ppm 100 mol % CF₃CF═CH₂, 63.6 87.5 27 ppm mol % HF, mol %  9.1 12.5 — Temp, ° C. — −17.2 −2.7 Pressure, psi — 24.7 (170) 26.7 (184) (kPa)

Example 22 Azeotropic Distillation for Separation of CF₃CH═CF₂ from CF₃CH₂CF₃

A mixture of HF, CF₃CH═CF₂, and CF₃CH₂CF₃ is fed to a distillation column for the purpose of purification of the CF₃CH═CF₂. The data in Table 24 were obtained by calculation using measured and calculated thermodynamic properties.

TABLE 24 Component or Column overhead variable Column feed (distillate) Column bottoms CF₃CH₂CF₃, 17.6 10 ppm 99.99 mol % CF₃CH═CF₂, 76.5 92.9 78 ppm mol % HF, mol %  5.9 7.1 — Temp, ° C. — −15.4 8.3 Pressure, psi — 19.7 (136) 21.7 (150) (kPa)

Example 23 Azeotropic Distillation for Separation of Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅ from C₂F₅CHFCHFCF₂C₂F₅

A mixture of HF, Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅, and C₂F₅CHFCHFCF₂C₂F₅ is fed to a distillation column for the purpose of purification of Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅. The data in Table 25 were obtained by calculation using measured and calculated thermodynamic properties.

TABLE 25 Column overhead Column Component or variable Column feed (distillate) bottoms C₂F₅CHFCHFCF₂C₂F₅, 33.4 1 ppm 100 mol % Z—C₂F₅CF═CHCF₂C₂F₅ 33.3 50.0 8 ppm and Z—C₂F₅CH═CFCF₂C₂F₅, mol % HF, mol % 33.3 50.0 — Temp, ° C. — 75.4 107 Pressure, psi (kPa) — 19.7 (136) 21.7 (150)

Example 24 Two-Column Azeotropic Distillation for Separation of E-CF₃CH═CHF from HF

A mixture of HF and E-CF₃CH═CHF is fed to a distillation set-up comprising 2 columns in series, the first at high pressure (HP) and the second at low pressure (LP). The data in Table 26 were obtained by calculation using measured and calculated thermodynamic properties. The numbers at the top of the columns refer to FIG. 1.

TABLE 26 570 585 540 Column 566 Column 586 Compound Feed (510) E—CF₃CH═CHF (520) HF or variable Mixture distillate product distillate product E—CF₃CH═CHF, 76.0 69.0 100 72.0 — mol % HF, mol % 24.0 31.0 — 28.0 100 Temp, ° C. — 68.6 76.1 −18.3   26.2 Pres, psi — 265 (1827) 267 (1841) 16.7 (115) 18.7 (129) (kPa)

Example 25 Two-Column Azeotropic Distillation for Separation of Z—CF₃CF═CHF from HF

A mixture of HF and Z—HFC-1225ye is fed to a distillation process for the purpose of purification of the Z—HFC-1225ye. The data in Table 27 were obtained by calculation using measured and calculated thermodynamic properties. The numbers at the top of the columns refer to FIG. 1.

TABLE 27 570 585 540 Column 566 Column 586 Compound or Feed (510) Z—CF₃CF═CHF (520) HF variable Mixture distillate product distillate product HF, mol % 26.7 35.0 trace 32.0 100 Z—CF₃CF═CHF, 73.3 65.0 100 68.0 — mol % Temp., ° C. — 76.6 86.0 −19.2 26.2 Pres., psi (kPa) — 334.7 (2307) 336.7 (2321) 16.7 (115) 18.7 (129)

Example 26 Two-Column Azeotropic Distillation for Separation of Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃ from HF

A mixture of HF and Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃ is fed to a distillation process for the purpose of purification of the Z—CF₃CH═CFCF₂CF₃ and Z—CF₃CF═CHCF₂CF₃. The data in Table 28 were obtained by calculation using measured and calculated thermodynamic properties. The numbers at the top of the columns refer to FIG. 1.

TABLE 28 570 585 586 540 Column 566 Column Z—CF₃CH═CFCF₂CF₃ Compound or Feed (510) HF (520) and Z—CF₃CF═CHCF₂CF₃ variable Mixture distillate product distillate product HF, mol % 73.9 70.0 100   82.5 100 Z—CF₃CH═CFCF₂CF₃ 26.1 30.0 — 17.5 — and Z—CF₃CF═CHCF₂CF₃, mol % Temp., ° C. — 91.7 117.5 14.9   39.8 Pres., psi (kPa) — 224.7 (1549) 226.7 (1563) 19.7 (136) 21.7 (150)

Example 27 Two-Column Azeotropic Distillation for Separation of CF₃CF═CH₂ from HF

A mixture of HF and CF₃CF═CH₂ is fed to a distillation process for the purpose of purification of the CF₃CF═CH₂. The data in Table 29 were obtained by calculation using measured and calculated thermodynamic properties. The numbers at the top of the columns refer to FIG. 1.

TABLE 29 570 585 Column 566 Column 586 Compound 540 (510) CF₃CF═CH₂ (520) HF or variable Feed Mixture distillate product distillate product HF, mol % 16.0 30.0 — 20.0 100 CF₃CF═CH₂, 84.0 70.0 100 80.0 — mol % Temp., — 71.2   80.2 −18.4   36.9 ° C. Pres., psi (kPa) — 364.7 (2515) 366.7 (2528) 24.7 (170) 26.7 (184)

Example 28 Two-Column Azeotropic Distillation for Separation of CF₃CH═CF₂ from HF

A mixture of HF and CF₃CH═CF₂ is fed to a distillation process for the purpose of purification of the CF₃CH═CF₂. The data in Table 30 were obtained by calculation using measured and calculated thermodynamic properties. The numbers at the top of the columns refer to FIG. 1.

TABLE 30 570 585 Column 566 Column 586 Compound 540 (510) CF₃CH═CF₂ (520) HF or variable Feed Mixture distillate product distillate product HF, mol % 30.4 24.1 — 30.5 100 CF₃CH═CF₂, 69.6 75.9 100 69.5 — mol % Temp., — 71.5   80.1 −17.1    30.6 ° C. Pres., — 314.7 (2170) 316.7 (2184) 19.7 (136) 21.7 (150) psi (kPa)

Example 29

Two-Column Azeotropic Distillation for Separation of Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅ from HF

A mixture of HF and Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅ is fed to a distillation process for the purpose of purification of the Z—C₂F₅CF═CHCF₂C₂F₅ and Z—C₂F₅CH═CFCF₂C₂F₅. The data in Table 31 were obtained by calculation using measured and calculated thermodynamic properties. The numbers at the top of the columns refer to FIG. 1.

TABLE 31 566 570 Z—C₂F₅CF═CHCF₂C₂F₅ 585 540 Column and Column 586 Compound or Feed (510) Z—C₂F₅CH═CFCF₂C₂F₅ (520) HF variable Mixture distillate product distillate product HF, mol % 93.9 95.8 100 91.0 100   Z—C₂F₅CF═CHCF₂C₂F₅  6.1  4.2 — 9.0 — and Z—C₂F₅CH═CFCF₂C₂F₅, mol % Temp., ° C. — 26.9   84.8 109 117.5 Pres., psi (kPa) — 19.7 (136) 21.7 (150) 224.7 (1549) 226.7 (1563)

Examples 30-33

Examples 30-33 use one of three reactors:

Reactor A: Inconel® 600 tube (this alloy is about 76 wt % nickel), 18 in (45.7 cm) long×1.0 in (2.5 cm) outer diameter×0.84 in (2.1 cm) inner diameter. Tube wall thickness is 0.16 in (0.41 cm). The preheat zone is 7 in (17.8 cm) long. The reaction zone is 2 in (5.1 cm) long. The quench zone is 7 in (17.8 cm) long. The tube is heated with 1 in (2.5 cm) diameter ceramic band heaters. The leads of a 7-point thermocouple are distributed long the length of the tube, with some in the middle of the reactor zone (to measure gas temperature). Reactor B: Schedule 80 Nickel 200 tube with an Inconel® 617 overlay, 18 in (45.7 cm) long, 1.5 in (3.8 cm) outer diameter, 0.84 in (2.1 cm) inner diameter. The reaction zone is 2 in (5.1 cm) long. The reactor zone is heated with an 8.5 in (21.6 cm) long×2.5 in (6.35 cm) split tube furnace. The leads of a 7-point thermocouple are distributed long the length of the tube, with some in the middle of the reactor zone (to measure gas temperature). Reactor C: Hastelloy® C276 with gold lining. Length 5 in (12.7 cm)×0.50 in (1.3 cm) outer diameter×0.35 in (0.89 cm) inner diameter. The wall thickness is 0.15 in (3.8 mm). The thickness of the gold lining is 0.03 in (0.08 cm). The reactor zone is 2 in (5.1 cm) long and is heated with a ceramic band heater.

Example 30

Reactor A (Inconel® 600 reaction surface) is used. The reactor inlet gas temperature (“Reactor Inlet T Gas” in Table 1) is the reaction temperature. Two runs are made at reaction temperatures of 724° C. and 725° C., respectively. In Run A, the reactant feed is undiluted with inert gas. In Run B, helium and reactant are fed in the ratio of 1.4:1. The benefit of the inert gas diluent is seen in the improved yield of Run B (80%) over that of Run A (71%). A lower concentration of fluorocarbon byproducts are made in Run B. Results are summarized in Table 32. Note that “sccm” in the table stands for “standard cubic centimeters per minute”.

TABLE 32 A B Reactor Conditions, Feeds Preheat Control T setting 700° C. 700° C. Preheat Gas T 1″ 545° C. 572° C. Preheat Gas T 2″ 635° C. 655° C. Preheat Gas T 3″ 690° C. 696° C. Preheat Gas T 4″ 718° C. 720° C. Reactor Control T setting 700° C. 700° C. Reactor Inlet T wall 711° C. 710° C. Reactor Middle T wall 700° C. 700° C. Reactor Exit T wall 622° C. 623° C. Reactor Inlet T gas 724° C. 725° C. Reactor Middle T gas 714° C. 716° C. Reactor Exit T gas 675° C. 673° C. HFC-236fa Feed sccm 25 sccm 25 sccm Helium Feed sccm  0 sccm 35 sccm Residence Time in Reaction Zone 42 18 (seconds) Gas Chromatograph Results in Mole % CHCF₃ (HFC-23) 4.5 2.1 CF₃CH═CF₂ (HFC-1225zc) 51.6 47.7 Octafluorocyclobutane (PFC-C318) 1.8 2.0 CF₃CH₂CF₃ (HFC-236fa) 27.5 40.3 C₄H₂F₆ (HFC-1336) 1.8 0.7 C₄HF₇ (HFC-1327) 1.7 1.2 C₄HF₉ (HFC-329) 4.2 2.1 Other 3.1 2.1 Unknown 3.8 1.8 Conversion (%) 72.5 59.7 Yield (%) 71 80

Example 31

Reactor A (Inconel® 600 reaction surface) is used in this study of the effect of temperature on conversion and yield. Run A is made at reactor temperature of 600° C. Runs B and C are made at 699° C. and 692° C., respectively. Runs A and B are diluted 4:1 with helium. Run C is undiluted. Run A (600° C.) conversion is low at 0.3%. Runs B and C (690-700° C.) have higher conversion, though still low compared to the conversion seen in Example 30, which was run at 725° C. and appreciably longer reaction zone residence times. Yields are reported, however are not reliable for such low conversions. The dependence of conversion on temperature and reaction zone residence time is plain from these experiments. Results are summarized in Table 33.

TABLE 33 A B C Reactor Conditions, Feeds Preheat Control T setting 600 700 700 (° C.) Preheat Gas T 1″ (° C.) 417 497 443 Preheat Gas T 2″ (° C.) 511 604 546 Preheat Gas T 3″ (° C.) 563 660 623 Preheat Gas T 4″ (° C.) 592 691 676 Reactor Control T setting 601 700 700 (° C.) Reactor Inlet T wall (° C.) 615 718 722 Reactor Middle T wall (° C.) 601 700 700 Reactor Exit T wall (° C.) 566 661 653 Reactor Inlet T gas (° C.) 600 699 692 Reactor Middle T gas (° C.) 588 684 665 Reactor Exit T gas (° C.) 560 650 609 Helium Feed sccm 400 400 0 HFC-236fa Feed sccm 100 100 200 Residence Time in Reaction 2 2 5 Zone (seconds) Gas Chromatograph Results in Mole % CHCF₃ (HFC-23) 0.0 0.0 0.1 CHF═CF₂ (HFC-1123) 0.0 0.0 0.1 CF₃CH═CF₂ (HFC-1225zc) 0.1 2.1 4.4 CF₃CH₂CF₃ (HFC-236fa) 99.7 97.6 95.3 Other (<1%) 0.2 0.2 0.3 Conversion (%) 0.3 2.4 4.7 Yield (%) 33 87.5 93.6

Example 32

Reactor B (Nickel 200 reaction surface) is used. In this reactor the reactor temperature is the reactor center gas temperature (“Reactor Center Gas T” in Table 3). Runs A, B, and C are made at 800° C. with helium:reactant ratios of 0:1, 1:1, and 2:1, respectively. At these temperatures, higher than in Example 30, and at comparable reaction zone residence times, on the nickel surface, conversions are as high, and yields higher. In pyrolyses, higher temperatures generally lead to lower yields because of increased rates of undesirable side reactions giving unwanted byproducts. That this is not seen in Example 32 is testimony to the superiority of the nickel reaction surface to the nickel alloy reaction surface of Example 30. Further support for this conclusion is found in Run D, made at 850° C. with 4:1 helium dilution. Conversion is high at 76.9%, and the yield is 90.5%, the best of any of the Example 32 runs. Results are summarized in Table 34.

TABLE 34 A B C D Reactor Conditions, Feeds Reactor Control T setting 839 834 832 885 (° C.) Reactor Inlet T wall (° C.) 812 806 804 853 Reactor Middle T wall (° C.) 831 826 824 877 Reactor Exit T wall (° C.) 808 805 804 855 Preheat Gas T 1″ (° C.) 658 666 669 707 Reactor Inlet gas T 2″ (° C.) 736 740 741 786 Reactor Inlet gas T 3″ (° C.) 779 780 781 829 Reactor Center gas T 4″ 800 800 800 850 (° C.) Reactor Exit gas T 5″ (° C.) 800 800 799 851 Reactor Exit gas T 6″ (° C.) 776 777 777 829 Exit gas T 7″ (° C.) 738 741 740 791 HFC-236fa Feed sccm 200 200 200 200 He Feed sccm 0 200 400 800 Residence Time in Reaction 5 3 2 1 Zone (seconds) GC Results in Mole % CHCF₃ (HFC-23) 4.1 2.5 2.0 2.5 CHF═CF₂ (HFC-1123) 0.7 1.0 1.0 1.4 CF₃CH═CF₂ (HFC-1225zc) 60.8 50.6 45.3 69.6 CF₃CH₂CF₃ (HFC-236fa) 28.2 37.7 50.2 23.1 C₄H₂F₆ (HFC-1336) 1.3 0.6 0.4 0.0 Other (<1% produced) 2.1 1.0 1.1 2.1 Unknown 2.8 6.6 0.0 1.2 Conversion (%) 71.8 62.3 49.8 76.9 Yield (%) 84.7 81.2 90.9 90.5

Example 33

Reactor C (gold reaction surface). Like nickel, the gold surface gives high yields and therefore reduced side reactions producing unwanted byproducts. The inert gas diluent effect (reduction) on conversion is less on gold than on nickel or nickel alloy surfaces. At 800° C. (Runs A and B) conversions are lower than those of Runs B and C of Example 32 but the average yield is higher. Results are summarized in Table 35.

TABLE 35 Reactor Conditions, Feeds A B C D E F Reactor Temp (° C.) 800 800 700 700 600 600 He Feed sccm 15 20 15 20 15 20 HFC-236fa Feed sccm 10 5 10 5 10 5 Residence Time in Reaction 8 8 8 8 8 8 Zone (seconds) GC Mole % CHF₃ and CH₂F₂ 1.9 1.9 0.1 0.1  ND* ND CHF═CF₂ (HFC-1123) 0.8 0.9 ND ND ND ND CF₃CH₃ (HFC-143a) 0.2 0.2 ND ND ND ND CF₃CH═CF₂ (HFC-1225zc) 33.3 36.6 1.7 1.8 0.2 0.1 CF₃CHFCF₃ (HFC-227ea) 0.2 0.2 0.1 0.1 0.1 0.1 CF₃CH₂CF₃ (HFC-236fa) 61.9 58.4 97.6 97.6 99.4 99.5 Unknown 0.6 0.5 0.3 0.1 0.2 0.1 Conversion (%) 38.1 41.6 2.4 2.4 0.6 0.5 Yield (%) 87.4 88.0 71 75 33 20 *ND = not detected

Examples 30-33 show the specificity of the pyrolysis according to this invention, which gives the product CF₃CH═CF₂ in good yield at good conversion with only small amounts of unwanted byproducts. Nickel is superior to nickel alloy as the reaction surface in giving higher yields of product. Gold is superior to nickel.

Conversions are low up to about 700° C., being good at 725° C. and above with no deterioration in performance even at 850° C. 

1. A process to produce 2,3,3,4,4,4-hexafluoro-1-butene comprising a) feeding 1,1,1,2,2,3,3-heptafluorobutane to a reaction zone containing a dehydrofluorination catalyst, thereby forming a product mixture comprising said 2,3,3,4,4,4-hexafluoro-1-butene, unreacted 1,1,1,2,2,3,3-heptafluorobutane and hydrogen fluoride, and b) recovering said 2,3,3,4,4,4-hexafluoro-1-butene from the product mixture produced in a).
 2. The process of claim 1, wherein said dehydrofluorination catalyst is chromium oxide, fluorided chromium oxide, cubic chromium trifluoride, fluorided alumina or aluminum fluoride.
 3. The process of claim 2, wherein said dehydrofluorination catalyst is chromium oxide, fluorided chromium oxide or cubic chromium trifluoride.
 4. The process of claim 1, wherein the dehydrofluorination is carried out at a temperature of from about 200° C. to about 500° C.
 5. The process of claim 1, wherein the dehydrofluorination is carried out at a temperature of from about 300° C. to about 450° C.
 6. The process of claim 1, wherein said 1,1,1,2,2,3,3-heptafluorobutane further comprised an inert diluent.
 7. The process of claim 6, wherein said inert diluent is nitrogen, helium or argon.
 8. The process of claim 7, wherein said inert diluent in nitrogen.
 9. The process of claim 8, wherein the mole ratio of 1,1,1,2,2,3,3-heptafluorobutane to nitrogen is from about 5:1 to about 1:1.
 10. The process of claim 1, wherein said product mixture is subjected to a first distillation step to form a first distillate composition comprising an azeotrope or near-azeotrope composition containing, 2,3,3,4,4,4-hexafluoro-1-butene and hydrogen fluoride and a first bottoms composition comprising 1,1,1,2,2,3,3-heptafluorobutane; Subjecting said first distillate composition to a second distillation step from which a composition enriched in either (i) hydrogen fluoride, or (ii) 2,3,3,4,4,4-hexafluoro-1-butene is removed as a second distillate composition with a second bottoms composition being enriched in the other of said components (i) or (ii); and Subjecting said second distillate composition to a third distillation step conducted at a different pressure than the second distillation step in which the component enriched in the second bottoms composition is removed as a third distillate composition with the third bottoms composition of the third distillation step enriched in the same component that was enriched in the second distillate composition.
 11. The process of claim 10, further comprising recycling at least some portion of said first bottoms composition to said reaction zone. 